Recombinant expression of factor VIII in human cells

ABSTRACT

The invention discloses a process for recombinant production of blood coagulation Factor VIII in an immortalized human embryonic retina cell, said cell expressing at least an adenoviral E1A protein and comprising a nucleic acid sequence encoding said Factor VIII, said nucleic acid sequence being under control of a heterologous promoter, said process comprising culturing said cell and expressing the Factor VIII in said cell, and harvesting the expressed Factor VIII. Cells that can be used in the process of the invention are also provided.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application is a continuation-in-part of co-pending U.S. patent application Ser. No. 10/234,007, filed Sep. 3, 2002, the contents of the entirety of which is incorporated by this reference, which is a divisional of U.S. patent application Ser. No. 09/549,463, filed Apr. 14, 2000, now U.S. Pat. No. 6,855,544, issued Feb. 15, 2005, the entire contents of which, including its sequence listing, is incorporated by this reference, which application claims priority under 35 U.S.C. Section 119(e) to Provisional Patent Application Ser. No. 60/129,452 filed Apr. 15, 1999.

STATEMENT ACCORDING 37 C.F.R. § 1.52(e)(5)—SEQUENCE LISTING SUBMITTED ON COMPACT DISC

Pursuant to 37 C.F.R. § 1.52(e)(1)(iii), a compact disc containing an electronic version of the Sequence Listing has been submitted concomitant with this application, the contents of which are hereby incorporated by reference. A second compact disc is submitted and is an identical copy of the first compact disc. The discs are labeled “copy 1” and “copy 2,” respectively, and each disc contains one file entitled “0034 D US P00 CIP seqlist.prj.ST25.txt” which is 99 KB and created on Nov. 15, 2005.

TECHNICAL FIELD

The invention relates generally to biotechnology and recombinant protein production, more particularly to the use of a human cell for the production of proteins. The invention is particularly useful for the production of proteins that benefit from post-translational or peri-translational modifications such as glycosylation and proper folding.

BACKGROUND

The expression of human recombinant proteins in heterologous cells has been well documented. Many production systems for recombinant proteins have become available, ranging from bacteria, yeasts, and fungi to insect cells, plant cells and mammalian cells. However, despite these developments, some production systems are still not optimal, or are only suited for production of specific classes of proteins. For instance, proteins that require post- or peri-translational modifications such as glycosylation, γ-carboxylation, or hydroxylation cannot be produced in prokaryotic production systems. Another well-known problem with prokaryotic expression systems is the incorrect folding of the product to be produced, even leading to insoluble inclusion bodies in many cases.

Eukaryotic systems are an improvement in the production of, in particular, eukaryote derived proteins, but the available production systems still suffer from a number of drawbacks. The hypermannosylation in, for instance, yeast strains affects the ability of yeasts to properly express glycoproteins. Hypermannosylation often even leads to immune reactions when a therapeutic protein thus prepared is administered to a patient. Furthermore, yeast secretion signals are different from mammalian signals, leading to a more problematic transport of mammalian proteins, including human polypeptides, to the extracellular, which in turn results in problems with continuous production and/or isolation. Mammalian cells are widely used for the production of such proteins because of their ability to perform extensive post-translational modifications. The expression of recombinant proteins in mammalian cells has evolved dramatically over the past years, resulting in many cases in a routine technology.

In particular, Chinese hamster ovary cells (“CHO cells”) have become a routine and convenient production system for the generation of biopharmaceutical proteins and proteins for diagnostic purposes. A number of characteristics make CHO cells very suitable as a host cell. The production levels that can be reached in CHO cells are extremely high. The cell line provides a safe production system, which is free of infectious or virus-like particles. CHO cells have been extensively characterized, although the history of the original cell line is vague. CHO cells can grow in suspension until reaching high densities in bioreactors, using serum-free culture media; a dhfr-mutant of CHO cells (DG-44 clone, Urlaub et al., 1983) has been developed to obtain an easy selection system by introducing an exogenous dhfr gene and thereafter a well-controlled amplification of the dhfr gene and the transgene using methotrexate.

However, glycoproteins or proteins comprising at least two (different) subunits continue to pose problems. The biological activity of glycosylated proteins can be profoundly influenced by the exact nature of the oligosaccharide component. The type of glycosylation can also have significant effects on immunogenicity, targeting and pharmacokinetics of the glycoprotein. In recent years, major advances have been made in the cellular factors that determine the glycosylation, and many glycosyl transferase enzymes have been cloned. This has resulted in research aimed at metabolic engineering of the glycosylation machinery (Fussenegger et al., 1999; Lee et al., 1989; Vonach et al., 1998; Jenikins et al., 1998; Zhang et al., 1998; Muchmore et al., 1989). Examples of such strategies are described herein.

CHO cells lack a functional α-2,6 sialyl-transferase enzyme, resulting in the exclusive addition of sialyc acids to galactose via α-2,3 linkages. It is known that the absence of α-2,6 linkages can enhance the clearance of a protein from the bloodstream. To address this problem, CHO cells have been engineered to resemble the human glycan profile by transfecting the appropriate glycosyl transferases. CHO cells are also incapable of producing Lewis X oligosaccharides. CHO cell lines have been developed that express human N-acetyl-D-glucosaminyltransferase and α-1,3-fucosyl-transferase III. In contrast, it is known that rodent cells, including CHO cells, produce CMP-N-acetylneuraminic acid hydrolase which lead to CMP-N-acetylneuraminic acids (Jenkins et al., 1996), an enzyme that is absent in humans. The proteins that carry this type of glycosylation can produce a strong immune response when injected (Kawashima et al., 1993). The recent identification of the rodent gene that encodes the hydrolase enzyme will most likely facilitate the development of CHO cells that lack this activity and will avoid this rodent-type modification.

Thus, it is possible to alter the glycosylation potential of mammalian host cells by expression of human glucosyl transferase enzymes. Yet, although the CHO-derived glycan structures on the recombinant proteins may mimic those present on their natural human counterparts, a potential problem exists in that they are still found to be far from identical. Another potential problem is that not all glycosylation enzymes have been cloned and are, therefore, available for metabolic engineering. The therapeutic administration of proteins that differ from their natural human counterparts may result in activation of the immune system of the patient and cause undesirable responses that may affect the efficacy of the treatment. Other problems using non-human cells may arise from incorrect folding of proteins that occurs during or after translation, which might be dependent on the presence of the different available chaperone proteins. Aberrant folding may occur, leading to a decrease or absence of biological activity of the protein. Furthermore, the simultaneous expression of separate polypeptides that will together form proteins comprised of the different subunits, like monoclonal antibodies, in correct relative abundancies is of great importance. Human cells will be better capable of providing all necessary facilities for human proteins to be expressed and processed correctly.

It would thus be desirable to have methods for producing human recombinant proteins that involve a human cell that provides consistent human-type processing like post-translational and peri-translational modifications, such as glycosylation, which preferably is also suitable for large-scale production.

SUMMARY OF THE INVENTION

Described are, among other things, methods and compositions for producing recombinant proteins in a human cell line. The methods and compositions are particularly useful for generating stable expression of human recombinant proteins of interest that are modified post-translationally, for example, by glycosylation. Such proteins are believed to have advantageous properties in comparison with their counterparts produced in non-human systems such as Chinese hamster ovary cells.

The invention thus provides a method for producing at least one proteinaceous substance in a cell including a eukaryotic cell having a sequence encoding at least one adenoviral E1 protein or a functional homologue, fragment and/or derivative thereof in its genome, which cell does not encode a structural adenoviral protein from its genome or a sequence integrated therein, the method including providing the cell with a gene encoding a recombinant proteinaceous substance, culturing the cell in a suitable medium and harvesting at least one proteinaceous substance from the cell and/or the medium. A proteinaceous substance is a substance including at least two amino-acids linked by a peptide bond. The substance may further include one or more other molecules physically linked to the amino acid portion or not. Non-limiting examples of such other molecules include carbohydrate and/or lipid molecules.

A nucleic acid sequence encoding an adenovirus structural protein should not be present for a number of reasons. One reason is that the presence of an adenoviral structural protein in a preparation of produced protein is highly undesired in many applications of such produced protein. Removal of the structural protein from the product is best achieved by avoiding its occurrence in the preparation. Preferably, the eukaryotic cell is a mammalian cell. In a preferred embodiment, the proteinaceous substance harvested from the cell and the cell itself is derived from the same species. For instance, if the protein is intended to be administered to humans, it is preferred that both the cell and the proteinaceous substance harvested from the cell are of human origin. One advantage of a human cell is that most of the commercially most attractive proteins are human.

The proteinaceous substance harvested from the cell can be any proteinaceous substance produced by the cell. In one embodiment, at least one of the harvested proteinaceous substances is encoded by the gene. In another embodiment, a gene is provided to the cell to enhance and/or induce expression of one or more endogenously present genes in a cell, for instance, by providing the cell with a gene encoding a protein that is capable of enhancing expression of a proteinaceous substance in the cell.

As used herein, a “gene” is a nucleic acid sequence including a nucleic acid sequence of interest in an expressible format, such as an expression cassette. The nucleic acid sequence of interest may be expressed from the natural promoter or a derivative thereof or an entirely heterologous promoter. The nucleic acid sequence of interest can include introns or not. Similarly, it may be a cDNA or cDNA-like nucleic acid. The nucleic acid sequence of interest may encode a protein. Alternatively, the nucleic acid sequence of interest can encode an anti-sense RNA.

The invention further provides a method for producing at least one human recombinant protein in a cell, including providing a human cell having a sequence encoding at least an immortalizing E1 protein of an adenovirus or a functional derivative, homologue or fragment thereof in its genome, which cell does not produce structural adenoviral proteins, with a nucleic acid encoding the human recombinant protein. The method involves culturing the cell in a suitable medium and harvesting at least one human recombinant protein from the cell and/or the medium. Until the present invention, few, if any, human cells exist that have been found suitable to produce human recombinant proteins in any reproducible and upscaleable manner. We have now found that cells which include at least immortalizing adenoviral E1 sequences in their genome are capable of growing (they are immortalized by the presence of E1) relatively independent of exogenous growth factors. Furthermore, these cells are capable of producing recombinant proteins in significant amounts and are capable of correctly processing the recombinant protein being made. Of course, these cells will also be capable of producing non-human proteins. The human cell lines that have been used to produce recombinant proteins in any significant amount are often tumor (transformed) cell lines. The fact that most human cells that have been used for recombinant protein production are tumor-derived adds an extra risk to working with these particular cell lines and results in very stringent isolation procedures for the recombinant protein in order to avoid transforming activity or tumorigenic material in any protein or other preparations. According to the invention, it is, therefore, preferred to employ a method wherein the cell is derived from a primary cell. In order to be able to grow indefinitely, a primary cell needs to be immortalized in some kind, which, in the present invention, has been achieved by the introduction of adenovirus E1.

BRIEF DESCRIPTION OF THE DRAWINGS

This patent or application file contains at least one drawing executed in color. Copies of this patent or patent application publication with color drawings will be provided by the Office upon request and payment of the necessary fee.

FIG. 1. Plasmid map of pCP-FactorVIII-FL and pCP-FactorVIII-SQ. See Example 35.

FIG. 2. Yields of Factor VIII-SQ produced in two serum-free media, ExCell Mab and ExCell VPRO, over an eight-hour culture period. See Example 37.

FIG. 3. Cell concentrations during each 24-hour culture period. See Example 38.

FIG. 4. Average Factor VIII production over 24-hour culture period. See Example 38.

FIG. 5. Plot of Factor VIII concentration against the integral of the viable cell concentration (IVC) (24-hour batch cultures). See Example 38.

FIG. 6. Cell concentrations during 24-hour culture period (with complete medium exchange at 2, 4 and 6 hours). See Example 38.

FIG. 7. Plot of FVIII concentration (average of 6×2-hour culture periods) against IVC. See Example 38.

DETAILED DESCRIPTION

In order to achieve large-scale (continuous) production of recombinant proteins through cell culture, it is preferred to have cells capable of growing without the necessity of anchorage. The cells of the present invention have that capability. The anchorage-independent growth capability is improved when the cells include a sequence encoding E2A or a functional derivative or analogue or fragment thereof in its genome, wherein preferably the E2A encoding sequence encodes a temperature sensitive mutant E2A, such as ts125. To have a clean, relatively safe production system from which it is easy to isolate the desired recombinant protein, it is preferred to have a method according to the invention, wherein the human cell includes no other adenoviral sequences. The most preferred cell for the methods and uses of the invention is PER.C6 as deposited under ECACC no. 96022940 or a derivative thereof (see, e.g., U.S. Pat. No. 5,994,128 to Fallaux et al. (Nov. 30, 1999), the contents of which are incorporated by this reference). PER.C6 cells behave better in handling than, for instance, transformed human 293 cells that have also been immortalized by the E1 region from adenovirus (Graham et al., 1977). PER.C6 cells have been characterized and have been documented very extensively because they behave significantly better in the process of upscaling, suspension growth and growth factor independence. Especially the fact that PER.C6 cells can be brought in suspension in a highly reproducible manner is something that makes it very suitable for large-scale production. Furthermore, the PER.C6 cell line has been characterized for bioreactor growth in which it grows to very high densities.

The cells according to the invention, in particular PER.C6 cells, have the additional advantage that they can be cultured in the absence of animal- or human-derived serum or animal- or human-derived serum components. Thus isolation is easier, while the safety is enhanced due to the absence of additional human or animal proteins in the culture, and the system is very reliable (synthetic media are the best in reproducibility). Furthermore, the presence of the Early region 1A (“E1A”) of adenovirus adds another level of advantages as compared to (human) cell lines that lack this particular gene. E1A as a transcriptional activator is known to enhance transcription from the enhancer/promoter of the CMV Immediate Early genes (Olive et al., 1990, Gorman et al., 1989). When the recombinant protein to be produced is under the control of the CMV enhancer/promoter, expression levels increase in the cells and not in cells that lack E1A.

In one aspect, the invention, therefore, further provides a method for enhancing production of a recombinant proteinaceous substance in a eukaryotic cell, including providing the eukaryotic cell with a nucleic acid encoding at least part of the proteinaceous substance, wherein the coding sequence is under control of a CMV-promoter, an E1A promoter or a functional homologue, derivative and/or fragment of either and further providing the cell with E1A activity or E1A-like activity. Like the CMV promoter, E1A promoters are more active in cells expressing one or more E1A products than in cells not expressing such products. It is known that indeed the E1A expression enhancement is a characteristic of several other promoters. For the present invention, such promoters are considered to be functional homologues of E1A promoters. The E1A effect can be mediated through the attraction of transcription activators, the E1A promoter or homologue thereof, and/or through the removal/avoiding attachment of transcriptional repressors to the promoter. The binding of activators and repressors to a promoter occurs in a sequence-dependent fashion. A functional derivative and/or fragment of an E1A promoter or homologue thereof, therefore, at least includes the nucleic acid binding sequence of at least one E1A protein regulated activator and/or repressor.

Another advantage of cells of the invention is that they harbor and express constitutively the adenovirus E1B gene. Adenovirus E1B is a well-known inhibitor of programmed cell death, or apoptosis. This inhibition occurs either through the 55K E1B product by its binding to the transcription factor p53 or subsequent inhibition (Yew and Berk 1992). The other product of the E1B region, 19K E1B, can prevent apoptosis by binding and thereby inhibiting the cellular death proteins Bax and Bak, both proteins that are under the control of p53 (White et al., 1992; Debbas and White, 1993; Han et al., 1996; and Farrow et al., 1995). These features can be extremely useful for the expression of recombinant proteins that, when over-expressed, might be involved in the induction of apoptosis through a p53-dependent pathway.

The invention further provides the use of a human cell for the production of a human recombinant protein, the cell having a sequence encoding at least an immortalizing E1 protein of an adenovirus or a functional derivative, homologue or fragment thereof in its genome, which cell does not produce structural adenoviral proteins. In another embodiment, the invention provides such a use wherein the human cell is derived from a primary cell, preferably wherein the human cell is a PER.C6 cell or a derivative thereof.

The invention further provides a use according to the invention, wherein the cell further includes a sequence encoding E2A or a functional derivative or analogue or fragment thereof in its genome, preferably wherein the E2A is temperature sensitive.

The invention also provides a human recombinant protein obtainable by a method according to the invention or by a use according to the invention, the human recombinant protein having a human glycosylation pattern different from the isolated natural human counterpart protein.

In another embodiment, the invention provides a human cell having a sequence encoding E1 of an adenovirus or a functional derivative, homologue or fragment thereof in its genome, which cell does not produce structural adenoviral proteins, and having a gene encoding a human recombinant protein, preferably a human cell which is derived from PER.C6 as deposited under ECACC no. 96022940.

In yet another embodiment, the invention provides such a human cell, PER.C6/E2A, which further includes a sequence encoding E2A or a functional derivative or analogue or fragment thereof in its genome, preferably wherein the E2A is temperature sensitive.

The proteins to be expressed in these cells using the methods of the invention are well known to persons skilled in the art. They are preferably human proteins that undergo some kind of processing in nature, such as secretion, chaperoned folding and/or transport, co-synthesis with other subunits, glycosylation, or phosphorylation. Typical examples for therapeutic or diagnostic use include monoclonal antibodies that are comprised of several subunits, tissue-specific plasminogen activator (“tPA”), granulocyte colony stimulating factor (“G-CSF”) and human erythropoietin (“EPO” or “hEPO”). EPO is a typical product that, especially in vivo, heavily depends on its glycosylation pattern for its activity and immunogenicity. Thus far, relatively high levels of EPO have been reached by the use of CHO cells which are differently glycosylated in comparison to EPO purified from human urine, albeit equally active in the enhancement of erythrocyte production. The different glycosylation of such EPO, however, can lead to immunogenicity problems and altered half-life in a recipient.

The present invention also includes a novel human immortalized cell line for this purpose and the uses thereof for production. PER.C6 cells (PCT International Patent Publication WO 97/00326 or U.S. Pat. No. 5,994,128) were generated by transfection of primary human embryonic retina cells using a plasmid that contained the adenovirus serotype 5 (Ad5) E1A- and E1B-coding sequences (Ad5 nucleotides 459-3510) under the control of the human phosphoglycerate kinase (“PGK”) promoter.

The following features make PER.C6 particularly useful as a host for recombinant protein production: (1) fully characterized human cell line; (2) developed in compliance with GRP; (3) can be grown as suspension cultures in defined serum-free medium devoid of any human- or animal-derived proteins; (4) growth compatible with roller bottles, shaker flasks, spinner flasks and bioreactors with doubling times of about 35 hours; (5) presence of E1A causing an up-regulation of expression of genes that are under the control of the CMV enhancer/promoter; (6) presence of E1B which prevents p53-dependent apoptosis possibly enhanced through overexpression of the recombinant transgene.

In one embodiment, the invention provides a method wherein the cell is capable of producing two- to 200-fold more recombinant protein and/or proteinaceous substance than conventional mammalian cell lines. Preferably, the conventional mammalian cell lines are selected from the group consisting of CHO, COS, Vero, Hela, BHK and Sp-2/0 cell lines.

Thus, it would be an improvement in the art to provide a human cell that produces consistent human-type protein processing like post-translational and peri-translational modifications, such as, but not limited to glycosylation. It would be further advantageous to provide a method for producing a recombinant mammalian cell and proteins from recombinant mammalian cells in large-scale production.

Previously, few, if any, human cells suitable for producing proteins in any reproducible and upscaleable manner have been found. The cells of the present invention include at least an immortalizing adenoviral E1 protein and are capable of growing relatively independent of exogenous growth factors.

Furthermore, these cells are capable of producing proteins in significant amounts and are capable of correctly processing the generated immunoglobulins.

The fact that cell types that have been used for protein production are tumor-derived adds an extra risk to working with these particular cell lines and results in very stringent isolation procedures for the proteins in order to avoid transforming activity or tumorigenic material in any preparations. It is, therefore, preferred to employ a method according to the invention, wherein the cell is derived from a primary cell. In order to be able to grow indefinitely, a primary cell needs to be immortalized, which in the present invention has been achieved by the introduction of an adenoviral E 1 protein.

In order to achieve large-scale (continuous) production of proteins through cell culture, it is preferred to have cells capable of growing without the necessity of anchorage. The cells of the present invention have that capability. The anchorage-independent growth capability is improved when the cells include an adenovirus-derived sequence encoding E2A (or a functional derivative or analogue or fragment thereof) in its genome. In a preferred embodiment, the E2A encoding sequence encodes a temperature sensitive mutant E2A, such as ts125. The cell may, in addition, include a nucleic acid (e.g., encoding tTa), which allows for regulated expression of a gene of interest when placed under the control of a promoter (e.g., a TetO promoter).

To have a clean and safe production system from which it is easy to isolate the desired proteins, it is preferred to have a method according to the invention, wherein the human cell includes no other adenoviral sequences. The most preferred cell for the methods and uses of the invention is a PER.C6 cell (or a derivative thereof) as deposited under ECACC no. 96022940. PER.C6 cells have been found to be more stable, particularly in handling, than, for instance, transformed human 293 cells immortalized by the adenoviral E1 region. PER.C6 cells have been extensively characterized and documented, demonstrating good process of upscaling, suspension growth and growth factor independence. Furthermore, PER.C6 can be incorporated into a suspension in a highly reproducible manner, making it particularly suitable for large-scale production. In this regard, the PER.C6 cell line has been characterized for bioreactor growth, where it can grow to very high densities.

The cells of the present invention, in particular PER.C6, can advantageously be cultured in the absence of animal- or human-derived serum, or animal- or human-derived serum components. Thus, isolation of proteins is simplified and safety is enhanced due to the absence of additional human or animal proteins in the culture. The absence of serum further increases reliability of the system since use of synthetic media, as contemplated herein, enhances reproducibility.

The invention further provides the use of a recombinant mammalian cell for the production of at least one polypeptide, the cell having a sequence encoding at least an immortalizing E1 protein of an adenovirus or a functional derivative, homologue or fragment thereof in its genome, which cell does not produce structural adenoviral proteins. In another embodiment, the invention provides such a use wherein the cell is derived from a primary cell, preferably wherein the human cell is a PER.C6 cell or a derivative thereof.

The invention further provides a use according to the invention, wherein the cell further includes a sequence encoding E2A (or a functional derivative or analogue or fragment thereof) in its genome, preferably wherein the E2A is temperature sensitive. In addition, the invention provides a method of using the invention, wherein the cell further includes a trans-activating protein for the induction of the inducible promoter. The invention also provides proteins obtainable by a method according to the invention or by a use according to the invention.

In another embodiment, the invention provides a human cell having a sequence encoding E1 of an adenovirus (or a functional derivative, homologue or fragment thereof) in its genome, which cell does not produce structural adenoviral proteins, and having a gene encoding a human recombinant protein, preferably a human cell which is derived from PER.C6 as deposited under ECACC No. 96022940.

In yet another embodiment, the invention provides such a human cell, PER.C6/E2A, which further includes a sequence encoding E2A (or a functional derivative, analogue or fragment thereof) in its genome, preferably wherein the E2A is temperature sensitive.

The present invention further provides methods for producing at least one polypeptide in a recombinant mammalian cell utilizing the immortalized recombinant mammalian cell of the invention, culturing the same in a suitable medium, and harvesting at least one polypeptide from the recombinant mammalian cell and/or medium. The recombinant polypeptides, or derivatives thereof, may be used for the therapeutic treatment of mammals or the manufacture of pharmaceutical compositions.

The preferred cell according to the invention is derived from a human primary cell, preferably a cell which is immortalized by a gene product of the E1 gene. In order to be able to grow, a primary cell, of course, needs to be immortalized. A good example of such a cell is one derived from a human embryonic retinoblast.

In cells according to the invention, it is important that the E1 gene sequences are not lost during the cell cycle. It is, therefore, preferred that the sequence encoding at least one gene product of the E1 gene is present in the genome of the (human) cell. For reasons of safety, care is best taken to avoid unnecessary adenoviral sequences in the cells according to the invention. It is thus another embodiment of the invention to provide cells that do not produce adenoviral structural proteins. However, in order to achieve large-scale (continuous) virus protein production through cell culture, it is preferred to have cells capable of growing without needing anchorage. The cells of the present invention have that capability. To have a clean and safe production system from which it is easy to recover and, if desirable, to purify the recombinant protein, it is preferred to have a method according to the invention, wherein the human cell includes no other adenoviral sequences. The most preferred cell for the methods and uses of the invention is PER.C6 as deposited under ECACC no. 96022940, or a derivative thereof.

Thus, the invention provides a method using a cell according to the invention, wherein the cell further includes a sequence encoding E2A or a functional derivative or analogue or fragment thereof, preferably a cell wherein the sequence encoding E2A or a functional derivative or analogue or fragment thereof is present in the genome of the human cell, and most preferably a cell wherein the E2A encoding sequence encodes a temperature sensitive mutant E2A.

Furthermore, as stated, the invention also provides a method according to the invention wherein the (human) cell is capable of growing in suspension.

The invention also includes a method wherein the human cell can be cultured in the absence of serum. The cells according to the invention, in particular PER.C6 cells, have the additional advantage that they can be cultured in the absence of serum or serum components. Thus, isolation is easy, safety is enhanced and reliability of the system is good (synthetic media are the best in reproducibility). The human cells of the invention, and in particular those based on primary cells and particularly the ones based on HER cells, are capable of normal post and peri-translational modifications and assembly. This means that they are very suitable for preparing proteins for use in therapeutic applications.

Thus, the invention also includes a method wherein the protein includes a protein that undergoes post-translational and/or peri-translational modification, especially wherein the modifications include glycosylation.

In another aspect, the invention provides the use of an adenoviral E1B protein or a functional derivative, homologue and/or fragment thereof having anti-apoptotic activity for enhancing the production of a proteinaceous substance in a eukaryotic cell, the use including providing the eukaryotic cell with the E1B protein, derivative, homologue and/or fragment thereof. In a preferred embodiment, the use includes a cell of the invention. In another preferred embodiment, the invention provides the use in a method and/or a use of the invention.

Factor VIII is a protein that participates in the intrinsic pathway of blood coagulation, where it is involved in the activation of Factor X to Factor Xa (reviewed in Bhopale and Nanda, 2003). Most patients suffering from the X-chromosome linked bleeding disorder Hemophilia A lack functional Factor VIII. Treatment consists of replacement therapy with plasma derived factor VIII or recombinant factor VIII from CHO or BHK cells expressing human factor VIII. Risk factors associated with the use of plasma-derived factor VIII including the transmission of TSE agents and viruses such as hepatitis and HIV are driving a move towards recombinant factor VIII. Issues surrounding the recombinant forms include most notably the production of sufficient quantities of functional factor VIII. Currently, marketed recombinant factor VIII is produced on the non-human CHO and BHK cell lines (for information concerning marketed factor VIII products, see BIOPHARMA: Biopharmaceutical Products in the U.S. Market, 3^(rd) Edition, Ronald Rader, Biotechnology Information Institute, Rockville Md., September 2004, entries 126-132; Ananyeva et al., 2004). Expression levels are low and production methods complex as a result of protein instability. Therefore, a need still exists for alternative expression methods for production of factor VIII.

U.S. Pat. No. 6,358,703 discloses a process for the production of proteins having factor VIII procoagulant activity at the industrial scale. Using a newly created cell host, HKB11 (a hybrid of human 293S cells and human Burkitt's lymphoma cells) cell clones with specific productivities in the range of 2 to 4 pg/cell/day (10 to 20 μU/c/d) were derived. Under serum-free conditions, one clone has sustained a daily productivity of 2 to 4 pg/c/d. Clones with this high level of productivity are able to produce 3 to 4 million units per day in a 15-liter perfusion fermentor. One unit of factor VIII activity is by definition the activity present in one milliliter of plasma. One pg of factor VIII is generally equivalent to about 5 μU of FVIII activity. The cells used therein are tumor-derived. Thus a need still exists for alternative expression methods for production of Factor VIII in cells that are not tumor-derived and that are well-documented to minimize safety concerns, while at the same time being capable of expressing Factor VIII at industrially feasible levels and with suitable glycosylation. The cells of the present invention have the advantage of not being tumor-derived but being derived from primary cells, and further are available well-documented and reportedly safe.

As shown in U.S. patent application Ser. No. 10/234,007 (the '007 application) of Bout et al., the contents of the entirety of which are incorporated by this reference, immortalized human embryonic retina cells expressing at least an adenovirus E1A protein can be suitably used for the production of recombinant proteins.

It is shown herein that these cells can be used for the recombinant expression of blood coagulation Factor VIII.

The present invention provides a process for producing Factor VIII in an immortalized human embryonic retina cell, said cell expressing at least an adenoviral E1A protein and expressing said Factor VIII from a nucleic acid sequence encoding said Factor VIII, said nucleic acid sequence being under control of a heterologous promoter, said process comprising: culturing said cell and allowing expression of the Factor VIII in said cell. Preferably, said cell further expresses at least one adenovirus E1B protein, e.g., E1B 55K and/or E1B 19K (the latter sometimes referred to as E1B 21 K in the literature). Preferably, said cell does not express an adenoviral structural protein. In a particularly preferred embodiment, the cell is a PER.C6 cell or originates from a PER.C6 cell. A PER.C6 cell according to this embodiment is a cell having the characteristics of the cells as deposited under ECACC no. 96022940. A cell originating from a PER.C6 cell according to this embodiment can be derived from a PER.C6 cell by introduction of the nucleic acid sequence encoding said Factor VIII under control of a heterologous promoter. In certain embodiments, the process is chosen from a batch, fed-batch, perfusion, and fed-perfusion process, and combinations of these.

The Factor VIII may be the full-length wild-type Factor VIII, of which a coding sequence is provided herein as SEQ ID NO:34. A sequence encoding factor VIII has for instance been disclosed in U.S. Pat. Nos. 4,757,006; 5,045,455; 5,633,150, all incorporated by reference in their entirety herein. Methods to recombinantly produce factor VIII have also been disclosed in these references. Factor VIII mRNA encodes a precursor protein of 2351 amino acids including a 19 amino acid signal peptide; thus the mature Factor VIII protein is 2332 amino acids long. The amino acid sequence predicted a domain structure consisting of a triplicated A domain, a unique B domain and a duplicated C domain arranged in the order A1, A2, B, A3, C1, C2. During coagulation the B domain is removed by thrombin activation of the molecule and its function is unknown.

Factor VIII thus comprises A, B and C domains, wherein the B domain is not essential for activity. The protein is sometimes referred to as split into a heavy and light chain, wherein the heavy chain may be a molecule of approximately 200 kDa, comprising amino acids 1 to 1648 (approximately coinciding with the A+B domains), or a 90 kDa fragment comprising amino acids 1 to 740 (approximately coinciding with the A domain, and missing largely the B-domain which comprises amino acids 741 to 1648), and wherein the light chain comprises an approximately 80 kDa fragment coinciding to a large extent with the C-domain (i.e., amino acids 1649 to 2332).

Characterization studies of recombinant human Factor VIII (D. L. Eaton, et al. (1987) J. Biol. Chem. 262, 3285-3290) showed that it is structurally and functionally very similar to plasma-derived Factor VIII. In plasma prepared in the presence of protease inhibitors, Factor VIII appeared as a complex of one heavy chain between 90 to 200 kDa (domains A1 and A2, with variable extensions of the B domain), in combination with one 80 kDa light chain (domains A3:C1:C2) (L. O. Andersson, et al. (1986) Proc. Natl. Acad. Sci. U.S.A. 83, 2979-2983). The chains could be dissociated by EDTA, indicating that they are held together by metal ions. The C-terminal part of the heavy chain, containing the heavily glycosylated B-domain, is shown to be very sensitive to proteolytic attack by serine proteases.

In preferred embodiments, the Factor VIII has a deletion in the B-domain (sometimes referred to as B-domain deleted Factor VIII, abbreviated as BDD-FVIII). B-domain deleted Factor VIII variants have been reported to be expressed 2 to 10 times better than full length Factor VIII in other cell lines (Herlitschka et al., 1998; Chen et al., 1999; Haack et al., 1999). Such truncated factor VIII mutants and recombinant expression thereof have for instance been disclosed in U.S. Pat. Nos. 4,868,112; 5,789,203, incorporated in their entirety by reference herein. In one embodiment, the Factor VIII with a deletion in the B-domain is the Factor VIII SQ mutant (EP Patents 0506757 and 0786474; Sandberg et al., 2001; for a review, see E. Bemtorp (1997) Thrombosis and Haemostasis 78, 256-260). The Factor VIII SQ protein consists of a 90 kDa heavy chain (domains A1:A2) and the 80 kDa light chain (domains A3:C1:C2), connected by a linker peptide The coding sequence of the Factor VIII SQ variant is provided herein as SEQ ID NO:36.

Of course, other variants of factor VIII can be produced as well, and are encompassed within the meaning of the term Factor VIII as used herein. Such variants can be prepared by the person skilled in the art by routine methods, e.g., by deletion, addition, substitution or combinations thereof of nucleotides in the sequences encoding factor VIII or BDD-FVIII, to create factor VIII wherein one or more amino acids are different from the full length or B-domain deleted factor VIII sequences as disclosed herein. Such factor VIII variants should still have procoagulant activity, i.e., are capable of activating factor X in an in vitro or in vivo model system, known to the person skilled in the art. Such variants have the capability of correcting factor VIII deficiencies, preferably in humans. Non-limiting examples of such factor VIII variants have been disclosed in for instance U.S. Pat. Nos. 5,171,844; 6,316,226; 6,346,513; 5,112,950; 5,422,260; 5,661,008; 5,859,204; 6,759,216; 6,770,744, and in WO 87/07144, U.S. 2004/0023333, EP 1424344; Pipe and Kaufman, 1997; Gale and Pellequer, 2003; all incorporated by reference herein. Preferably, the variants have an amino acid sequence that has not more than 10% amino acid substitutions compared to the sequences disclosed herein under SEQ ID NOS:35 and 37 (representing the full length wild-type Factor VIII and the SQ mutant Factor VIII amino acid sequences, respectively).

It is disclosed herein that B-domain deleted Factor VIII can be expressed in PER.C6 cells at relatively high levels of more than 3 Units/10⁶ cells/day. The invention, therefore, also provides a process according to the invention, wherein the specific productivity of Factor VIII with a deletion in the B-domain is at least 0.1 Unit/10⁶ million cells/day, preferably at least 0.2 Unit/10 million cells/day, more preferably at least 0.5 Unit/10 million cells/day, still more preferably at least 1.0 Unit/10 million cells/day, even more preferably at least 2, 3 or 5 Units/10 million cells/day. It is expected that the specific productivity will typically not be higher than 50, more typically not higher than 20 Units/10 million cells/day. The specific activity of the produced factor VIII may be determined by means known in the art, e.g., by using the commercially available COATEST assay (Coatest Factor VIII, Chromogenix AB, Molndal, Sweden; e.g., U.S. Pat. Nos. 5,851,800; 5,952,198; 6,346,513; Herlitschka et al., 1998; Cho and Chan, 2002; Pipe and Kaufman, 1997). In short, activated factor X (Xa) is generated via the intrinsic pathway where factor VIII acts as co-factor. Factor Xa is then determined by the use of a synthetic chromogenic substrate, S-2222 in the presence of a thrombin inhibitor I-2581 to prevent hydrolysis of the substrate by thrombin. The reaction is stopped with acid, and the VIII:C, which is proportional to the release of pNA (para-nitroaniline), is determined photometrically at 450 nm against a reagent blank. The unit of factor VIII:C is expressed in international units (IU) as defined by the current International Concentrate Standard (IS) established by WHO. Levels of Factor VIII may also be measured using for instance an ELISA, as known to the person skilled in the art. Another assay for Factor VIII activity is the so-called APTT (Activated Partial Thromboplastin Time) test, which is a standard coagulation assay known to the person skilled in the art (e.g., U.S. Pat. No. 6,346,513; Gale and Pellequer, 2003; Pipe and Kaufman, 1997; Sandberg et al., 2001).

The invention also provides the cells that can be used in the methods of the invention. The invention, therefore, also provides an immortalized human embryonic retina cell, comprising: a genome; a nucleic acid sequence encoding an adenoviral E1A protein, wherein the nucleic acid sequence encoding the adenoviral E1A protein is integrated in the genome; and a nucleic acid sequence encoding blood coagulation Factor VIII under control of a heterologous promoter, wherein the nucleic acid sequence encoding blood coagulation Factor VIII under control of a heterologous promoter is integrated in the genome of the immortalized human embryonic retina cell. These cells are to be used for the recombinant production of Factor VIII according to the invention.

Preferably, the sequences encoding adenoviral E1A and E1B proteins in the cells of the invention do not encode further any structural adenovirus proteins, such as pIX. Suitable constructs to provide sequences encoding adenoviral E1A and E1B proteins have for instance been described in U.S. Pat. No. 5,994,128, incorporated by reference herein, and include for instance pIG.E1A.E1B therein comprising nucleotides 459 to 3510 of the human adenovirus 5 genome (SEQ ID NO:33), which encode E1A and E1B but lack sequences from the pIX gene, which encodes a structural adenoviral protein. Another example of suitable sequences encoding adenoviral E1A and E1B protein comprises nt 505-3522 of human Ad5, such as present in STK146 as described in U.S. Pat. No. 6,558,948. Preferably, the E1A region is under control of a heterologous promoter, such as a phosphoglycerate kinase (PGK) promoter (e.g., U.S. Pat. Nos. 5,994,128 and 6,558,948), to drive expression of E1A in the cells. Preferably, said cells do not comprise any sequences encoding adenovirus structural proteins in their genome. It is further preferred that no adenovirus structural proteins are expressed or present in the cells. Preferably, the nucleic acid sequence encoding adenoviral E1A and E1B proteins is integrated into the genome of the HER cell. This ensures stable inheritance of the E1 sequence such that it can be expressed continuously and therewith contributes to the permanent character of the cell line, since adenovirus E1 sequences contribute to or are even responsible for the immortalization, so that a permanent “selection” for immortalization and hence continuous growth capacity is present.

Methods to produce proteins in host cells are well established and known to the person skilled in the art. The use of immortalized HER cells for this purpose is described in the incorporated '007 application. The present invention discloses the production of Factor VIII, further according to the teachings of that application.

In general, the production of a recombinant protein, such as Factor VIII, in a host cell comprises the introduction of nucleic acid in expressible format into the host cell, culturing the cells under conditions conducive to expression of the nucleic acid and allowing expression of the said nucleic acid in said cells. For the purpose of this application “express,” “expressing” or “expression” refers to the transcription and translation of a gene encoding a protein.

Alternatively, a protein that is naturally expressed in desired host cells, but not at sufficient levels, may be expressed at increased levels by introducing suitable regulation sequences such as a strong promoter in operable association with the desired gene (see, e.g., WO 99/05268, where the endogenous EPO gene is overexpressed by introduction of a strong promoter upstream of the gene in human cells). This could also be done for Factor VIII using the cells of the invention.

Preferably, the nucleic acid encoding the Factor VIII is integrated into the genome of the cell according to the invention. This ensures that the nucleic acid is stably inherited to the progeny of the cells and, therefore, can still be expressed after many cell generations.

The sequence encoding the Factor VIII polypeptide (or protein, or proteinaceous molecule, the terms are used interchangeably herein) encodes a mammalian Factor VIII protein, preferably the human Factor VIII protein, or a mutein thereof that is still functional in the blood coagulation cascade. The sequence of Factor VIII is available in the art (supra). Such sequences can now routinely be cloned from various sources, and/or partly or wholly synthesised, cloned in operable association with a promoter that is functional in eukaryotic cells, all with routine molecular biology methods known to the person skilled in the art.

Nucleic acid encoding a protein in expressible format may be in the form of an expression cassette, and usually requires sequences capable of bringing about expression of the nucleic acid, such as enhancer(s), promoter, polyadenylation signal, and the like. Several promoters can be used for expression of recombinant nucleic acid, and these may comprise viral, mammalian, synthetic promoters, and the like. In certain embodiments, a promoter driving the expression of the nucleic acid of interest is the cytomegalovirus (CMV) immediate early promoter, for instance comprising nt. −735 to +95 from the CMV immediate early gene enhancer/promoter, as this promoter has been shown to give high expression levels in cells expressing E1A of an adenovirus such as the cells of the invention (see, e.g., WO 03/051927). The nucleic acid encoding Factor VIII may be a genomic DNA, a cDNA, synthetic DNA, a combination of these, etc. Preferably, the nucleic acid encoding Factor VIII is a cDNA. If desired, one or more artificial or natural introns may be re-inserted into the cDNA (see, e.g., EP 1283263). It is also possible to remove cryptic splice sites to enhance the expression (see, e.g., U.S. Pat. No. 6,642,028). Codons may be optimized if desired to improve expression (see, e.g., U.S. Pat. No. 6,114,148).

Some well-known and much used promoters for expression in eukaryotic cells comprise promoters derived from viruses, such as adenovirus, e.g., the E1A promoter, promoters derived from cytomegalovirus (CMV), such as the CMV immediate early (1E) promoter (referred to herein as the CMV promoter) (obtainable, for instance, from pcDNA, Invitrogen), promoters derived from Simian Virus 40 (SV40) (Das et al., 1985), and the like. Suitable promoters can also be derived from eukaryotic cells, such as methallothionein (MT) promoters, elongation factor 1α (EF-1α) promoter (Gill et al., 2001), ubiquitin C or UB6 promoter (Gill et al., 2001; Schorpp et al., 1996), actin promoter, an immunoglobulin promoter, heat shock promoters, and the like. Some preferred promoters for obtaining expression in eukaryotic cells, which are suitable promoters in the present invention, are the CMV-promoter, a mammalian EF1-alpha promoter, a mammalian ubiquitin promoter such as a ubiquitin C promoter, or a SV40 promoter (e.g., obtainable from pIRES, cat. no. 631605, BD Sciences). Testing for promoter function and strength of a promoter is a matter of routine for a person skilled in the art, and in general may for instance encompass cloning a test gene such as lacZ, luciferase, GFP, etc., behind the promoter sequence, and test for expression of the test gene. Of course, promoters may be altered by deletion, addition, mutation of sequences therein, and tested for functionality, to find new, attenuated, or improved promoter sequences. Strong promoters that give high transcription levels in the eukaryotic cells of the invention are preferred.

Introduction of the nucleic acid that is to be expressed in a cell, can be done by one of several methods, which as such are known to the person skilled in the art, also dependent on the format of the nucleic acid to be introduced. Said methods include but are not limited to transfection, infection, injection, transformation, and the like. Preferably, clones resulting from single cells are obtained and subsequently used for expression of Factor VIII.

The terms “cell culture medium” and “culture medium” refer to a nutrient solution used for growing mammalian cells that typically provides at least one component from one or more of the following categories: 1) an energy source, usually in the form of a carbohydrate such as glucose; 2) all essential amino acids, and usually the basic set of twenty amino acids plus cysteine; 3) vitamins and/or other organic compounds required at low concentrations; 4) free fatty acids; and 5) trace elements, where trace elements are defined as inorganic compounds or naturally occurring elements that are typically required at very low concentrations, usually in the micromolar range. The nutrient solution may optionally be supplemented with one or more components from any of the following categories: 1) hormones and other growth factors as, for example, insulin, transferrin, and epidermal growth factor; 2) salts and buffers as, for example, calcium, magnesium, and phosphate; 3) nucleosides and bases such as, for example, adenosine, thymidine, and hypoxanthine; and 4) protein and tissue hydrolysates. Cell culture media are available from various vendors, and serum-free culture media are nowadays often used for cell culture, because they are more defined than media containing serum. The cells of the present invention grow well in serum-containing media as well as in serum-free media. Usually some time is required to adapt the cells from a serum containing medium, such as DMEM+FBS, to a serum-free medium. One example of a serum-free culture medium that is suitable for use in the present invention is EX-CELLTM VPRO medium (JRH Biosciences, catalog number 14561). The cells of the invention in general grow adherently in serum-containing media, but are very proficient in growing in suspension to high cell densities (10×10⁶ cells/ml and higher) in serum-free culture media, which means that they do not need a surface to adhere to, but remain relatively free from each other and from the walls of the culture vessel during most of the time. Processes for culturing the cells of the invention to high densities and/or for obtaining very high product yields from these cells have been described (WO 2004/099396), incorporated herein by reference. Culturing a cell is done to enable it to metabolize, and/or grow and/or divide and/or produce recombinant proteins of interest. This can be accomplished by methods well known to persons skilled in the art, and includes but is not limited to providing nutrients for the cell. The methods comprise growth adhering to surfaces, growth in suspension, or combinations thereof. Culturing can be done for instance in dishes, roller bottles or in bioreactors, using batch, fed-batch, continuous systems such as perfusion systems, and the like. In order to achieve large scale (continuous) production of recombinant proteins through cell culture it is preferred in the art to have cells capable of growing in suspension, and it is preferred to have cells capable of being cultured in the absence of animal- or human-derived serum or animal- or human-derived serum components. The conditions for growing or multiplying cells (see, e.g., Tissue Culture, Academic Press, Kruse and Paterson, editors (1973)) and the conditions for expression of the recombinant product are known to the person skilled in the art. In general, principles, protocols, and practical techniques for maximizing the productivity of mammalian cell cultures can be found in Mammalian Cell Biotechnology: a Practical Approach (M. Butler, ed., IRL Press, 1991).

It is, of course, also possible to co-express a protein that is beneficial to the activity, stability, yield and/or quality of the expressed Factor VIII. It will for instance be appreciated by the person skilled in the art that von Willebrand Factor (vWF) can be co-expressed with Factor VIII (see, e.g., U.S. Pat. No. 5,198,349), using the cells of the invention. Alternatively, vWF may be added to the culture medium during culturing or harvesting of Factor VIII (see, e.g., EP 0251843). In such embodiments, the von Willebrand factor is preferably used in an amount of 10 to 100, more preferably 50 to 60 mol vWF per mol factor VIII (in the culture broth and/or in the factor VIII solution during the purification procedure). Further, during culturing of the cells and/or harvest of the Factor VIII protein according to the invention, additives such as stabilizing compounds, e.g., recombinant hSA, and/or protease inhibitors (see, e.g., U.S. Pat. No. 5,851,800), and the like may be added. Other additives that may be used in the production of Factor VIII include phospholipids (U.S. Pat. No. 5,250,421), divalent metal ions such as Ca²⁺, Zn²⁺, Cu²⁺ and Mn²⁺ (WO 01/03726), polyols such as Pluronic F-68 (U.S. Pat. No. 5,804,420) and lipids/liposomes (U.S. Pat. No. 5,952,198). Furthermore, Factor VIII has a complex glycosylation pattern with many possibilities for the addition of a terminal sialic acid to the N-glycans and, therefore, it is also possible to further co-express a glycosyltransferase, preferably a sialyltransferase, such as an α2,6-sialyltransferase or an α2,3-sialyltransferase in the cells of the invention. Means and methods to establish such have been disclosed in U.S. patent application Ser. Nos. 11/026,518 (published as U.S. 2005/0164386) and 11/102,073 (published as U.S. 2005/0181359), incorporated in their entirety by reference herein.

The Factor VIII protein may be produced by growing the cells of the present invention that express the desired protein under a variety of cell culture conditions. For instance, cell culture procedures for the large or small-scale production of proteins are potentially useful within the context of the present invention. Procedures including, but not limited to, a fluidized bed bioreactor, hollow fiber bioreactor, roller bottle culture, or stirred tank bioreactor system may be used, in the later two systems, with or without microcarriers, and operated alternatively in a batch, fed-batch, or continuous mode.

In certain embodiments the cell culture of the present invention is performed in a stirred tank bioreactor system and a batch or a fed batch culture procedure is employed. In the fed batch culture the mammalian host cells and culture medium are supplied to a culturing vessel initially and additional culture nutrients are fed, continuously or in discrete increments, to the culture during culturing, with or without periodic cell and/or product harvest before termination of culture. The fed batch culture can include, for example, a semi-continuous fed batch culture, wherein periodically whole culture (including cells and medium) is removed and replaced by fresh medium. Fed batch culture is distinguished from simple batch culture in which all components for cell culturing (including the cells and all culture nutrients) are supplied to the culturing vessel at the start of the culturing process. Fed batch culture can be further distinguished from perfusion culturing insofar as the supernate is not removed from the culturing vessel during the process (in perfusion culturing, the cells are restrained in the culture by, e.g., filtration, encapsulation, anchoring to microcarriers, etc., and the culture medium is continuously or intermittently introduced and removed from the culturing vessel). Feed strategies for fed-batch cultures of the cells of the invention have been disclosed in WO 2004/099396, incorporated herein by reference. In that patent application, it was also disclosed that the cells of the present invention can grow to very high viable cell densities, far above 10×10⁶ cells/ml. This can be beneficially used for a perfusion process. In certain embodiments, the process is a perfusion process. A perfusion process is particularly advantageous for production of Factor VIII because Factor VIII is degraded in the culture medium. In a perfusion process, the produced Factor VIII is in the culture for shorter periods than in corresponding (fed-)batch processes and, therefore, suffers less from degradation. Suitable perfusion processes for the cells of the invention are for instance disclosed in WO 2005/095578, incorporated by reference herein. In perfusion processes for producing factor VIII using the cells and methods of the invention, the perfusion rate may for instance be chosen at suitable points in the range between 0.5 and 20 culture volumes per 24 hours, and cell densities may be used varying for instance between 5 and 100×10⁶ cells/ml.

The Factor VIII protein may be expressed intracellularly, but preferably is secreted into the culture medium. Naturally secreted proteins, such as Factor VIII, contain secretion signals that bring about secretion of the produced proteins. In a preferred embodiment, the expressed Factor VIII protein is collected (isolated), either from the cells or from the culture medium or from both. The Factor VIII thus preferably is recovered from the culture medium as a secreted polypeptide. For example, as a first step, the culture medium or lysate is centrifuged to remove particulate cell debris. The polypeptide thereafter is preferably purified from contaminant soluble proteins and polypeptides, e.g., by filtration, column chromatography, etc, by methods generally known to the person skilled in the art. Suitable purification steps include methods which were known in the art can be used to maximize the yield of a pure, stable and highly active product and are selected from immunoaffinity chromatography, anion exchange chromatography, size exclusion chromatography, etc., and combinations thereof. In particular, detailed purification protocols for coagulation factors from human blood plasma are, e.g., disclosed in WO93/15105, EP0813597, WO96/40883 and WO 96/15140/50. They can easily be adapted to the specific requirements needed to isolate recombinant factor VIII. Several methods to purify factor VIII have been reported, e.g., in U.S. Pat. Nos. 6,005,082; 6,143,179; 5,659,017; 5,288,853; 5,259,951; 4,578,218 and, e.g., in EP 1414857. The person skilled in the art can use a suitable method from these reported methods, or make modifications to optimize such methods for the purification of Factor VIII according to routine experimentation. Further methods are disclosed in the patents and applications relating to recombinant production of Factor VIII (supra) and to the formulation of Factor VIII (infra).

To overcome the problems of possible infectious contaminations in the purified protein samples or in the product directly obtained from the cell culture supernatant containing the secreted recombinant protein of choice, the samples and/or the culture supernatant might be treated with procedures for virus inactivation including heat treatment (dry or in liquid state, with or without the addition of chemical substances including protease inhibitors). After virus inactivation a further purifying step for removing the chemical substances may be necessary. In particular, for factor VIII isolated from blood plasma the recovery of a high purity virus-inactivated protein by anion exchange chromatography was described (WO93/15105). In addition several processes for the production of high-purity, non-infectious coagulation factors from blood plasma or other biological sources have been reported. Lipid coated viruses are effectively inactivated by treating the potentially infectious material with a hydrophobic phase forming a two-phase system, from which the water-insoluble part is subsequently removed. A further advantage has been proven to complement the hydrophobic phase treatment simultaneously or sequentially with a treatment with non-ionic biocompatible detergents and dialkyl or trialkyl phosphates. (WO 9636369, EP0131740, U.S. Pat. No. 6,007,979.) Non-lipid coated viruses require inactivation protocols consisting in treatment with non-ionic detergents followed by a heating step (60 to 65° C.) for several hours (WO94/17834). The cells of the invention are available free of adventitious virus and TSE and a well-documented history is available for these cells, so that they can be used to produce Factor VIII in a safe manner.

Factor VIII as produced using the methods of the invention can be part of pharmaceutical compositions, can be used for preparing medicaments for treating hemophilia and can be applied in methods for treating hemophilia. The above pharmaceutical compositions and the above medicaments may comprise the factor VIII in a therapeutically effective dose, e.g., from 50 to 500 μg (with 200 ng factor VIII corresponding to one International Unit (IU)). Depending on the type of hemophilia, a patient receives an annual dose of factor VIII of up to 200,000 IU, which is usually administered in weekly or twice weekly doses.

The pharmaceutical compositions, medicaments or preparations applied in methods for treating hemophilia contain a therapeutically effective dose of the factor VIII, and usually at least one pharmaceutically acceptable carrier or excipient. Pharmaceutically suitable formulations of Factor VIII can be prepared according to methods known to the person skilled in the art (see Remington's Pharmaceutical Sciences, 18th edition, A. R. Gennaro, Ed., Mack Publishing Company (1990); Pharmaceutical Formulation Development of Peptides and Proteins, S. Frokjaer and L. Hovgaard, Eds., Taylor & Francis (2000); and Handbook of Pharmaceutical Excipients, 3rd edition, A. Kibbe, Ed., Pharmaceutical Press (2000)). Several formulations of Factor VIII have been described (see, e.g., U.S. Pat. Nos. 5,733,873; 5,919,766; 5,972,885; 5,925,739; 6,649,386; 5,919,908; 6,586,573; 6,599,724; and EP 1016673, EP 1308170; EP 1079805; EP 1194161; WO 03/080108; U.S. Pat. No. 5,698,677; U.S. Pat. No. 6,228,613; U.S. 2001/0007766; WO 03/066681).

To illustrate the invention, the following examples are provided, not intended to limit the scope of the invention. The human erythropoietin (EPO) molecule contains four carbohydrate chains. Three contain N-linkages to asparagines, and one contains an O-linkage to a serine residue. The importance of glycosylation in the biological activity of EPO has been well documented (Delorme et al., 1992; Yamaguchi et al., 1991). The cDNA encoding human EPO was cloned and expressed in PER.C6 cells and PER.C6/E2A cells, expression was shown, and the glycosylation pattern was analyzed.

The practice of this invention will employ, unless otherwise indicated, conventional techniques of immunology, molecular biology, microbiology, cell biology, and recombinant DNA, which are within the skill of the art. See, e.g., Sambrook, Fritsch and Maniatis, Molecular Cloning: A Laboratory Manual, 2nd edition, 1989; Current Protocols in Molecular Biology, F. M. Ausubel, et al., eds, 1987; the series Methods in Enzymology (Academic Press, Inc.); PCR2: A Practical Approach, M. J. MacPherson, B. D. Hams, G. R. Taylor, eds, 1995; Antibodies: A Laboratory Manual, Harlow and Lane, eds, 1988.

EXAMPLES Example 1

Construction of Basic Expression Vectors

Plasmid pcDNA3.1/Hygro(−) (Invitrogen) was digested with NruI and EcoRV, dephosphorylated at the 5′ termini by Shrimp Alkaline Phosphatase (SAP, GIBCO Life Tech.) and the plasmid fragment lacking the immediate early enhancer and promoter from CMV was purified from gel. Plasmid pAdApt.TM. (Crucell N V of Leiden, NL), containing the full length CMV enhancer/promoter (−735 to +95) next to overlapping Adeno-derived sequences to produce recombinant adenovirus, was digested with AvrII, filled in with Klenow polymerase and digested with HpaI; the fragment containing the CMV enhancer and promoter was purified over agarose gel. This CMV enhancer and promoter fragment was ligated bluntiblunt to the NruI/EcoRV fragment from pcDNA3.1/Hygro(−). The resulting plasmid was designated pcDNA2000/Hyg(−).

Plasmid pcDNA2000/Hyg(−) was digested with PmlI, and the linearized plasmid lacking the Hygromycin resistance marker gene was purified from gel and religated. The resulting plasmid was designated pcDNA2000. Plasmid pcDNA2000 was digested with PmlI and dephosphorylated by SAP at both termini. Plasmid pIG-GC9 containing the wild-type human DHFR cDNA (Havenga et al., 1998) was used to obtain the wild-type DHFR-gene by polymerase chain reaction (PCR) with introduced, noncoding PmlI sites upstream and down stream of the cDNA. PCR primers that were used were DHFR up: 5′-GAT CCA CGT GAG ATC TCC ACC ATG GTT GGT TCG CTA AAC TG-3′ (SEQ ID NO:1), corresponding to the SEQUENCE LISTING of U.S. patent application Ser. No. 10/234,007 (the '007 application) of Bout et al., the contents of the entirety of which are incorporated by this reference) and DHFR down: 5′-GAT CCA CGT GAG ATC TTT AAT CAT TCT TCT CAT ATAC-3′ (SEQ ID NO:2) corresponding to the incorporated '007 application. The PCR-product was digested with PmlI and used for ligation into pcDNA2000 (digested with PmlI, and dephosphorylated by SAP) to obtain pcDNA2000/DHFRwt (FIG. 1 of the incorporated '007 application). Wild-type sequences and correctly used cloning sites were confirmed by double stranded sequencing. Moreover, a mutant version of the human DHFR gene (DHFRm) was used to reach a 10,000-fold higher resistance to methotrexate in PER.C6 and PER.C6/E2A by selection of a possible integration of the transgene in a genomic region with high transcriptional activity. This mutant carries an amino acid substitution in position 32 (phenylalanine to serine) and position 159 (leucine to proline) introduced by the PCR procedure. PCR on plasmid pIG-GC12 (Havenga et al., 1998) was used to obtain the mutant version of human DHFR. Cloning of this mutant is comparable to wild-type DHFR. The plasmid obtained with mutant DHFR was designated pcDNA2000/DHFRm.

pIPspAdapt 6 (Galapagos Genomics of Belgium) was digested with AgeI and BamHI restriction enzymes. The resulting polylinker fragment has the following sequence: 5′-ACC GGT GAA TTC GGC GCG CCG TCG ACG ATA TCG ATC GGA CCG ACG CGT TCG CGA GCG GCC GCA ATT CGC TAG CGT TAA CGG ATC C-3′ (SEQ ID NO:3) corresponding to the incorporated '007 application. The used AgeI and BamHI recognition sites are underlined. This fragment contains several unique restriction enzyme recognition sites and was purified over agarose gel and ligated to an AgeI/BamHI-digested and agarose gel-purified pcDNA2000/DHFRwt plasmid. The resulting vector was named pcDNA2001/DHFRwt (FIG. 2 of the incorporated '007 application).

pIPspAdapt7 (Galapagos of Belgium) is digested with AgeI and BamHI restriction enzymes and has the following sequence: 5′-ACC GGT GAA TTG CGG CCG CTC GCG AAC GCG TCG GTC CGT ATC GAT ATC GTC GAC GGC GCG CCG AAT TCG CTA GCG TTA ACG GAT CC-3′ (SEQ ID NO:4) corresponding to the incorporated '007 application. The used AgeI and BamHI recognition sites are underlined in the incorporated '007 application. The polylinker fragment contains several unique restriction enzyme recognition sites (different from pIPspAdapt6), which are purified over agarose gel and ligated to an AgeI/BamHI-digested and agarose gel-purified pcDNA2000/DHFRwt. This results in pcDNA2002/DHFRwt (FIG. 3 of the incorporated '007 application).

pcDNA2000/DHFRwt was partially digested with restriction enzyme PvuII. There are two PvuII sites present in this plasmid and cloning was performed into the site between the SV40 poly(A) and ColE1, not the PvuII site down stream of the BGH poly(A). A single site-digested mixture of plasmid was dephosphorylated with SAP and blunted with Klenow enzyme and purified over agarose gel. pcDNA2000/DHFRwt was digested with MunI and PvuII restriction enzymes and filled in with Klenow and free nucleotides to have both ends blunted. The resulting CMV promoter-linker-BGH poly(A)-containing fragment was isolated over gel and separated from the vector. This fragment was ligated into the partially digested and dephosphorylated vector and checked for orientation and insertion site. The resulting plasmid was named pcDNAs3000/DHFRwt (FIG. 4 of the incorporated '007 application).

Example 2

Construction of EPO Expression Vectors

The full length human EPO cDNA was cloned, employing oligonucleotide primers EPO-START: 5′ AAA AAG GAT CCG CCA CCA TGG GGG TGC ACG AAT GTC CTG CCT G-3′ (SEQ ID NO:5) corresponding to the incorporated '007 application and EPO-STOP: 5′-AAA AAG GAT CCT CAT CTG TCC CCT GTC CTG CAG GCC TC-3′ (SEQ ID NO:6) corresponding to the incorporated '007 application (Cambridge Bioscience Ltd.) in a PCR on a human adult liver cDNA library. The amplified fragment was cloned into pUC18 linearized with BamHI. Sequence was checked by double stranded sequencing. This plasmid containing the EPO cDNA in pUC18 was digested with BamHI and the EPO insert was purified from agarose gel. Plasmids pcDNA2000/DHFRwt and pcDNA2000/DHFRm were linearized with BamHI and dephosphorylated at the 5′ overhang by SAP, and the plasmids were purified from agarose gel. The EPO cDNA fragment was ligated into the BamHI sites of pcDNA2000/DHFRwt and pcDNA2000/DHFRm; the resulting plasmids were designated pEPO2000/DHFRwt (FIG. 5 of the incorporated '007 application) and pEPO2000/DHFRm.

The plasmid pMLPI.TK (described in PCT International Patent Publication No. WO 97/00326) is an example of an adapter plasmid designed for use in combination with improved packaging cell lines like PER.C6 (described in PCT International Patent Publication No. WO 97/00326 and U.S. Pat. No. 6,033,908 to Bout et al. (Mar. 7, 2000), the contents of both of which are incorporated by this reference). First, a PCR fragment was generated from pZipDMo+PyF101(N−) template DNA (described in International Patent Application No. PCT/NL96/00195) with the following primers: LTR-1 (5′-CTG TAC GTA CCA GTG CAC TGG CCT AGG CAT GGA AAA ATA CAT AAC TG-3′ (SEQ ID NO:7) corresponding to the incorporated '007 application and LTR-2 (5′-GCG GAT CCT TCG AAC CAT GGT AAG CTT GGT ACC GCT AGC GTT AAC CGG GCG ACT CAG TCA ATC G-3′ (SEQ ID NO:8) corresponding to the incorporated '007 application). The PCR product was then digested with BamHI and ligated into pMLP10 (Levrero et al., 1991), that was digested with PvuII and BamHI, thereby generating vector pLTR10. This vector contains adenoviral sequences from bp 1 up to bp 454 followed by a promoter consisting of a part of the Mo-MuLV LTR having its wild-type enhancer sequences replaced by the enhancer from a mutant polyoma virus (PyF10). The promoter fragment was designated L420. Next, the coding region of the murine HSA gene was inserted. pLTR10 was digested with BstBI followed by Klenow treatment and digestion with NcoI. The HSA gene was obtained by PCR amplification on pUC18-HSA (Kay et al., 1990, using the following primers: HSAI (5′-GCG CCA CCA TGG GCA GAG CGA TGG TGG C-3′ (SEQ ID NO:9) corresponding to the incorporated '007 application) and HSA2 (5′-GTT AGA TCT AAG CTT GTC GAC ATC GAT CTA CTA ACA GTA GAG ATG TAG AA-3′ (SEQ ID NO:10) corresponding to the incorporated '007 application). The 269 bp PCR fragment was subcloned in a shuttle vector using NcoI and BglII sites. Sequencing confirmed incorporation of the correct coding sequence of the HSA gene, but with an extra TAG insertion directly following the TAG stop codon. The coding region of the HSA gene, including the TAG duplication, was then excised as a NcoI/SalI fragment and cloned into a 3.5 kb NcoI/BstBI cut pLTR10, resulting in pLTR-HSA10. This plasmid was digested with EcoRI and BamHI, after which the fragment, containing the left ITR, the packaging signal, the L420 promoter and the HSA gene, was inserted into vector pMLPI.TK digested with the same enzymes and thereby replacing the promoter and gene sequences, resulting in the new adapter plasmid pAd5/L420-HSA.

The pAd5/L420-HSA plasmid was digested with AvrII and BglII followed by treatment with Klenow and ligated to a blunt 1570 bp fragment from pcDNA1/amp (Invitrogen) obtained by digestion with HhaI and AvrII followed by treatment with T4 DNA polymerase. This adapter plasmid was named pAd5/CLIP.

To enable removal of vector sequences from the left ITR, pAd5/L420-HSA was partially digested with EcoRI and the linear fragment was isolated. An oligo of the sequence 5′ TTA AGT CGA C-3′ (SEQ ID NO:11) corresponding to the incorporated '007 application was annealed to itself, resulting in a linker with a SalI site and EcoRI overhang. The linker was ligated to the partially digested pAd5/L420-HSA vector and clones were selected that had the linker inserted in the EcoRI site 23 bp upstream of the left adenovirus ITR in pAd5/L420-HSA, resulting in pAd5/L420-HSA.sal.

To enable removal of vector sequences from the left ITR, pAd5/CLIP was also partially digested with EcoRI and the linear fragment was isolated. The EcoRI linker 5′ TTA AGT CGA C-3′ (SEQ ID NO:12) corresponding to the incorporated '007 application was ligated to the partially digested pAd5/CLIP vector and clones were selected that had the linker inserted in the EcoRI site 23 bp upstream of the left adenovirus ITR, resulting in pAd5/CLIP.sal. The vector pAd5/L420-HSA was also modified to create a Pacd site upstream of the left ITR. Hereto, pAd5/L420-HSA was digested with EcoRI and ligated to a Pacd linker (5′-AAT TGT CTT AAT TAA CCG CTT AA-3′ (SEQ ID NO:13) corresponding to the incorporated '007 application). The ligation mixture was digested with Pacd and religated after isolation of the linear DNA from agarose gel to remove concatamerized linkers. This resulted in adapter plasmid pAd5/L420-HSA.pac.

This plasmid was digested with AvrII and BglII. The vector fragment was ligated to a linker oligonucleotide digested with the same restriction enzymes. The linker was made by annealing oligos of the following sequence: PLL-1 (5′-GCC ATC CCT AGG AAG CTT GGT ACC GGT GAA TTC GCT AGC GTT AAC GGA TCC TCT AGA CGA GAT CTG G-3′ (SEQ ID NO:14) corresponding to the incorporated '007 application) and PLL-2 (5′-CCA GAT CTC GTC TAG AGG ATC CGT TAA CGC TAG CGA ATT CAC CGG TAC CAA GCT TCC TAG GGA TGG C-3′ (SEQ ID NO:15) corresponding to the incorporated '007 application). The annealed linkers were separately ligated to the AvrII/BglII-digested pAd5/L420-HSA.pac fragment, resulting in pAdMire.pac. Subsequently, a 0.7 kb ScaI/BsrGI fragment from pAd5/CLIP.sal containing the sal linker was cloned into the ScaI/BsrGI sites of the pAdMire.pac plasmid after removal of the fragment containing the pac linker. This resulting plasmid was named pAdMire.sal.

Plasmid pAd5/L420-HSA.pac was digested with AvrII and 5′ protruding ends were filled in using Klenow enzyme. A second digestion with HindIII resulted in removal of the L420 promoter sequences. The vector fragment was isolated and ligated separately to a PCR fragment containing the CMV promoter sequence. This PCR fragment was obtained after amplification of CMV sequences' from pCMVLacI (Stratagene) with the following primers: CMVplus (5′-GAT CGG TAC CAC TGC AGT GGT CAA TAT TGG CCA TTA GCC-3′ (SEQ ID NO:16) corresponding to the incorporated '007 application) and CMVminA (5′-GAT CAA GCT TCC AAT GCA CCG TTC CCG GC-3′ (SEQ ID NO:17) corresponding to the incorporated '007 application). The PCR fragment was first digested with PstI after which the 3′-protruding ends were removed by treatment with T4 DNA polymerase. Then the DNA was digested with HindIII and ligated into the AvrII/HindIII-digested pAd5/L420-HSA.pac vector. The resulting plasmid was named pAd5/CMV-HSA.pac. This plasmid was then digested with HindIII and BamHI and the vector fragment was isolated and ligated to the HindIII/BglII polylinker sequence obtained after digestion of pAdMire.pac. The resulting plasmid was named pAdApt.pac and contains nucleotides −735 to +95 of the human CMV promoter/enhancer (M. Boshart et al., 1985).

The full length human EPO cDNA (Genbank accession number: MI 1319) containing a perfect Kozak sequence for proper translation was removed from the pUC18 backbone after a BamHI digestion. The cDNA insert was purified over agarose gel and ligated into pAdApt.pac, which was also digested with BamHI, subsequently dephosphorylated at the 5′ and 3′ insertion sites using SAP and also purified over agarose gel to remove the short BamHI-BamHI linker sequence. The obtained circular plasmid was checked with KpnI, DdeI and NcoI restriction digestions that all gave the right size bands. Furthermore, the orientation and sequence was confirmed by double stranded sequencing. The obtained plasmid with the human EPO cDNA in the correct orientation was named pAdApt.EPO (FIG. 6 of the incorporated '007 application).

Example 3

Construction of UBS-54 Expression Vectors

The constant domains (CH1, −2 and −3) of the heavy chain of the human immunoglobulin G1 (IgG1) gene including intron sequences and connecting (“Hinge”) domain were generated by PCR using an upstream and a down stream primer. The sequence of the upstream primer (CAMH-UP) is 5′-GAT CGA TAT CGC TAG CAC CAA GGG CCC ATC GGT C-3′ (SEQ ID NO:18) corresponding to the incorporated '007 application, in which the annealing nucleotides are depicted in italics and two sequential restriction enzyme recognition sites (EcoRV and NheI) are underlined.

The sequence of the down stream primer (CAMH-DOWN) is: 5′-GAT CGT TTA AAC TCA TTT ACC CGG AGA CAG-3′ (SEQ ID NO:19) corresponding to the incorporated '007 application, in which the annealing nucleotides are depicted in italics and the introduced PmeI restriction enzyme recognition site is underlined.

The order in which the domains of the human IgG1 heavy chain were arranged is as follows: CH1-intron-Hinge-intron-CH2-intron-CH3. The PCR was performed on a plasmid (pCMgamma NEO Skappa Vgamma Cgamma hu) containing the heavy chain of a humanized antibody directed against D-dimer from human fibrinogen (Vandamme et al., 1990). This antibody was designated “15C5” and the humanization was performed with the introduction of the human constant domains including intron sequences (Bulens et al., 1991). The PCR resulted in a product of 1621 nucleotides. The NheI and PmeI sites were introduced for easy cloning into the pcDNA2000/Hyg(−) polylinker. The NheI site encoded two amino acids (Ala and Ser) that are part of the constant region CH1, but that did not hybridize to the DNA present in the template (Crowe et al., 1992).

The PCR product was digested with NheI and PmeI restriction enzymes, purified over agarose gel and ligated into a NheI and PmeI-digested and agarose gel-purified pcDNA2000/Hygro(−). This resulted in plasmid pHC2000/Hyg(−) (FIG. 7 of the incorporated '007 application), which can be used for linking the human heavy chain constant domains, including introns to any possible variable region of any identified immunoglobulin heavy chain for humanization.

The constant domain of the light chain of the human immunoglobulin (IgG1) gene was generated by PCR using an upstream and a down stream primer: The sequence of the upstream primer (CAML-UP) is 5′-GAT CCG TAC GGT GGC TGCACCATC TGT C-3′ (SEQ ID NO:20) corresponding to the incorporated '007 application, in which the annealing nucleotides are depicted in italics and an introduced SunI restriction enzyme recognition site is underlined.

The sequence of the down stream primer (CAML-DOWN) is 5′-GAT CGT TTA AAC CTA ACA CTC TCC CCT GTT G-3′ (SEQ ID NO:21) corresponding to the incorporated '007 application, in which the annealing nucleotides are in italics and an introduced PmeI restriction enzyme recognition site is underlined.

The PCR was performed on a plasmid (pCMkappa DHFR13 15C5 kappa humanized) carrying the murine signal sequence and murine variable region of the light chain of 15C5 linked to the constant domain of the human IgG1 light chain (Vandamme et al., 1990; Bulens et al., 1991).

The PCR resulted in a product of 340 nucleotides. The. SunI and PmeI sites were introduced for cloning into the pcDNA2001/DHFRwt polylinker. The SunI site encoded two amino acids (Arg and Thr) of which the threonine residue is part of the constant region of human immunoglobulin light chains, while the arginine residue is part of the variable region of CAMPATH-1H (Crowe et al., 1992). This enabled subsequent 3′ cloning into the SunI site, which was unique in the plasmid.

The PCR product was digested with SunI and PmeI restriction enzymes purified over agarose gel, ligated into a BamHI, PmeI-digested, and agarose gel-purified pcDNA2001/DHFRwt, which was blunted by Klenow enzyme and free nucleotides. Ligation in the correct orientation resulted in loss of the BamHI site at the 5′ end and preservation of the SunI and PmeI sites. The resulting plasmid was named pLC2001/DHFRwt (FIG. 8 of the incorporated '007 application), which plasmid can be used for linking the human light chain constant domain to any possible variable region of any identified immunoglobulin light chain for humanization.

pNUT-C gamma (Huls et al., 1999) contains the constant domains, introns and hinge region of the human IgG1 heavy chain (Huls et al., 1999) and received the variable domain upstream of the first constant domain. The variable domain of the gamma chain of fully humanized monoclonal antibody UBS-54 is preceded by the following leader peptide sequence: MACPGFLWALVISTCLEFSM (SEQ ID NO:22) corresponding to the incorporated '007 application (sequence: 5′-ATG GCA TGC CCT GGC TTC CTG TGG GCA CTT GTG ATC TCC ACC TGT CTT GAA TTT TCC ATG-3′) (SEQ ID NO:23) corresponding to the incorporated '007 application. This resulted in an insert of approximately 2 kb in length. The entire gamma chain was amplified by PCR using an upstream primer (UBS-UP) and the down stream primer CAMH-DOWN. The sequence of UBS-UP is as follows: 5′-GAT CAC GCG TGC TAG CCA CCA TGG CAT GCC CTG GCT TC-3′ (SEQ ID NO:24) corresponding to the incorporated '007 application in which the introduced MluI and NheI sites are underlined and the perfect Kozak sequence is italicized.

The resulting PCR product was digested with NheI and PmeI restriction enzymes, purified over agarose gel and ligated to the pcDNA2000/Hygro(−) plasmid that is also digested with NheI and PmeI, dephosphorylated with tSAP and purified over gel. The resulting plasmid was named pUBS-Heavy2000/Hyg(−) (FIG. 9 of the incorporated '007 application). pNUT-C kappa contains the constant domain of the light chain of human IgG1 kappa (Huls et al., 1999) and received the variable domain of fully humanized monoclonal antibody UBS-54 kappa chain preceded by the following leader peptide: MACPGFLWALVISTCLEFSM (SEQ ID NO:25) corresponding to the incorporated '007 application (sequence: 5′-ATG GCA TGC CCT GGC TTC CTG TGG GCA CTT GTG ATC TCC ACC TGT CTT GAA TTT TCC ATG -3′ (SEQ ID NO:26) corresponding to the incorporated '007 application, for details on the plasmid see U-BiSys of Utrecht, NL). This resulted in an insert of approximately 1.2 kb in length.

The entire insert was amplified by PCR using the upstream primer UBS-UP and the down stream primer CAML-DOWN, hereby modifying the translation start site. The resulting PCR product was digested with NheI and PmeI restriction enzymes, purified over agarose gel and ligated to pcDNA2001/DHFRwt that was also digested with NheI and PmeI, dephosphorylated by tSAP and purified over gel, resulting in pUBS-Light2001/DHFRwt (FIG. 10 of the incorporated '007 application). To remove the extra intron which is located between the variable domain and the first constant domain that is present in pNUT-Cgamma and to link the signal peptide and the variable domain to the wild-type constant domains of human IgG1 heavy chain, lacking a number of polymorphisms present in the carboxy-terminal constant domain in pNUT-Cgamma, a PCR product is generated with primer UBS-UP and primer UBSHV-DOWN that has the following sequence: 5′-GAT CGC TAG CTG TCGAGA CGG TGA CCA G-3′ (SEQ ID NO:27) corresponding to the incorporated '007 application, in which the introduced NheI site is underlined and the annealing nucleotides are italicized. The resulting PCR product is digested with NheI restriction enzyme, purified over gel and ligated to a NheI-digested and SAP-dephosphorylated pHC2000/Hyg(−) plasmid that was purified over gel. The plasmid with the insert in the correct orientation and reading frame is named pUBS2-Heavy2000/Hyg(−) (FIG. 11 of the incorporated '007 application).

For removal of an extra intron which is located between the variable domain and the constant domain that is present in pNUT-Ckappa and to link the signal peptide and the variable domain to the wild-type constant domain of human IgG1 light chain, a PCR product was generated with primer UBS-UP and primer UBSLV-DOWN that has the following sequence: 5′-GAT CCG TAC GCT TGA TCT CCA CCT TGG TC-3′ (SEQ ID NO:28) corresponding to the incorporated '007 application, in which the introduced SunI site is underlined and the annealing nucleotides are in bold. Then the resulting PCR product was digested with MluI and SunI restriction enzymes, purified over gel and ligated to a MluI and SunI-digested pLC2001/DHFRwt plasmid that was purified over gel. The resulting plasmid was named pUBS2-Light2001/DHFRwt (FIG. 12 of the incorporated '007 application).

The PCR product of the full-length heavy chain of UBS-54 is digested with NheI and PmeI restriction enzymes and blunted with Klenow enzyme. This fragment is ligated to the plasmid pcDNAs3000/DHFRwt that is digested with BstXI restriction enzyme, blunted, dephosphorylated by SAP and purified over gel. The plasmid with the heavy chain insert is named pUBS-Heavy3000/DHFRwt. Subsequently, the PCR of the light chain is digested with MluI and PmeI restriction enzymes, blunted, purified over gel and ligated to pUBS-Heavy3000/DHFRwt that is digested with HpaI, dephosphorylated by tSAP and purified over gel. The resulting vector is named pUBS-3000/DHFRwt (FIG. 13 of the incorporated '007 application). The gene that encodes the heavy chain of UBS-54 without an intron between the variable domain and the first constant region and with a wild-type carboxy terminal constant region (2031 nucleotides) is purified over gel after digestion of pUBS2-2000/Hyg(−) with EcoRI and PmeI and treatment with Klenow enzyme and free nucleotides to blunt the EcoRI site. Subsequently, the insert is ligated to a pcDNAs3000/DHFRwt plasmid that is digested with BstXI, blunted, dephosphorylated with SAP and purified over gel. The resulting plasmid is named pUBS2-Heavy3000/DHFRwt. pUBS2-Light2001/DHFRwt is then digested with EcoRV and PmeI, and the 755 nucleotide insert containing the signal peptide linked to the variable domain of the kappa chain of UBS-54 and the constant domain of human IgG1 kappa chain without an intron sequence is purified over gel and ligated to pUBS2-Heavy3000/DHFRwt that is digested with HpaI, dephosphorylated with tSAP and purified over gel. The resulting plasmid is named pUBS2-3000/DHFRwt (FIG. 14 of the incorporated '007 application).

Plasmid pRc/CMV (Invitrogen) was digested with BstBI restriction enzymes, blunted with Klenow enzyme and subsequently digested with XmaI enzyme. The Neomycin resistance gene containing fragment was purified over agarose gel and ligated to pUBS-Light2001/DHFRwt plasmid that was digested with XmaI and PmlI restriction enzymes, followed by dephosphorylation with SAP and purified over gel to remove the DHFR cDNA. The resulting plasmid was named pUBS-Light2001/Neo(−). The fragment was also ligated to a XmaI/PmlI-digested and gel-purified pcDNA2001/DHFRwt plasmid resulting in pcDNA2001/Neo. The PCR product of the UBS-54 variable domain and the digested and purified constant domain PCR product were used in a three-point ligation with a MluI/PmeI-digested pcDNA2001/Neo. The resulting plasmid was named pUBS2-Light2001/Neo.

Example 4

Construction of CAMPATH-1H Expression Vectors

Cambridge Bioscience Ltd. (UK) generates a 396 nucleotide fragment containing a perfect Kozak sequence followed by the signal sequence and the variable region of the published CAMPATH-1H light chain (Crowe et al., 1992). This fragment contains, on the 5′ end, an introduced and unique HindIII site and, on the 3′ end, an introduced and unique SunI site and is cloned into an appropriate shuttle vector. This plasmid is digested with HindIII and SunI and the resulting CAMPATH-1H light chain fragment is purified over gel and ligated into a HindIII/SunI-digested and agarose gel-purified pLC2001/DHFRwt. The resulting plasmid is named pCAMPATH-Light2001/DHFRwt. Cambridge Bioscience Ltd. (UK) generated a 438 nucleotide fragment containing a perfect Kozak sequence followed by the signal sequence and the published variable region of the CAMPATH-1H heavy chain (Crowe et al., 1992), cloned into an appropriate cloning vector. This product contains a unique HindIII restriction enzyme recognition site on the 5′ end and a unique NheI restriction enzyme recognition site on the 3′ end. This plasmid was digested with HindIII and NheI and the resulting CAMPATH-1H heavy chain fragment was purified over gel and ligated into a purified and HindIII/NheI-digested pHC2000/Hyg(−). The resulting plasmid was named pCAMPATH-Heavy2000/Hyg(−).

Example 5

Construction of 15C5 Expression Vectors

The heavy chain of the humanized version of the monoclonal antibody 15C5 directed against human fibrin fragment D-dimer (Bulens et al., 1991; Vandamme et al., 1990) consisting of human constant domains including intron sequences, hinge region and variable regions preceded by the signal peptide from the 15C5 kappa light chain is amplified by PCR on plasmid “pCMgamma NEO Skappa Vgamma Cgamma hu” as a template using CAMH-DOWN as a down stream primer and 15C5-UP as the upstream primer. 15C5-UP has the following sequence: 5′-GA TCA CGC GTG CTA GCC ACC ATG GGT ACT CCT GCT CAG TTT CTT GGA ATC-3′ (SEQ ID NO:29) corresponding to the incorporated '007 application, in which the introduced MluI and NheI restriction recognition sites are underlined and the perfect Kozak sequence is italicized. To properly introduce an adequate Kozak context, the adenine at position +4 (the adenine in the ATG start codon is +1) is replaced by a guanine, resulting in a mutation from an arginine into a glycine amino acid. To prevent primer dimerization, position +6 of the guanine is replaced by a thymine and the position +9 of the cytosine is replaced by thymine. This latter mutation leaves the threonine residue intact. The resulting PCR was digested with NheI and PmeI restriction enzymes, purified over gel and ligated to a NheI and PmeI-digested pcDNA2000/Hygro(−), that is dephosphorylated by SAP and purified over agarose gel. The resulting plasmid is named p15C5-Heavy20000/Hyg(−). The light chain of the humanized version of the monoclonal antibody 15C5 directed against human fibrin fragment D-dimer (Bulens et al., 1991; Vandamme et al., 1990) consisting of the human constant domain and variable regions preceded by a 20 amino acid signal peptide is amplified by PCR on plasmid pCMkappa DHFR13 15C5kappa hu as a template, using CAML-DOWN as a down stream primer and 15C5-UP as the upstream primer. The resulting PCR is digested with NheI and PmeI restriction enzymes, purified over gel and ligated to an NheI and PmeI-digested pcDNA2001/DHFRwt that is dephosphorylated by SAP and purified over agarose gel. The resulting plasmid is named p15C5-Light2001/DHFRwt.

Example 6

Establishment of Methotrexate Hygromycin and G418 Selection Levels.

PER.C6 and PER.C6/E2A were seeded in different densities. The starting concentration of methotrexate (MTX) in these sensitivity studies ranged between 0 nM and 2500 nM. The concentration which was just lethal for both cell lines was determined; when cells were seeded in densities of 100,000 cells per well in a six-well dish, wells were still 100% confluent at 10 nM and approximately 90 to 100% confluent at 25 nM, while most cells were killed at a concentration of 50 nM and above after six days to 15 days of incubation. These results are summarized in Table 1 of the incorporated '007 application. PER.C6 cells were tested for their resistance to a combination of Hygromycin and G418 to select outgrowing stable colonies that expressed both heavy and light chains for the respective recombinant monoclonal antibodies encoded by plasmids carrying either a hygromycin or a neomycin resistance gene. When cells were grown on normal medium containing 100 μg/ml hygromycin and 250 μg/ml G418, non-transfected cells were killed and stable colonies could appear. (See, Example 7.)

CHO-dhfr cells ATCC deposit CRL9096 are seeded in different densities in their respective culture medium. The starting concentration of methotrexate in these sensitivity studies ranges from approximately 0.5 nM to 500 nM. The concentration, which is just lethal for the cell line, is determined and subsequently used directly after growth selection on hygromycin in the case of IgG heavy chain selection (hyg) and light chain selection (dhfr).

Example 7

Transfection of EPO Expression Vectors to Obtain Stable Cell Lines

Cells of cell lines PER.C6 and PER.C6/E2A were seeded in 40-tissue culture dishes (10 cm diameter) with approximately 2 to 3 million cells/dish and were kept overnight under their respective conditions (10% CO₂ concentration and temperature, which is 39° C. for PER.C6/E2A and 37° C. for PER.C6). The next day, transfections were all performed at 37° C. using Lipofectamine (Gibco). After replacement with fresh (DMEM) medium after four hours, PER.C6/E2A cells were transferred to 39° C. again, while PER.C6 cells were kept at 37° C. Twenty dishes of each cell line were transfected with 5 μg ScaI-digested pEPO2000/DHFRwt and twenty dishes were transfected with 5 μg ScaI-digested pEPO2000/DHFRm, all according to standard protocols. Another 13 dishes served as negative controls for methotrexate killing and transfection efficiency, which was approximately 50%. On the next day, MTX was added to the dishes in concentrations ranging between 100 and 1000 nM for DHFRwt and 50,000 and 500,000 nM for DHFRm dissolved in medium containing dialyzed FBS. Cells were incubated over a period of four to five weeks. Tissue medium (including MTX) was refreshed every two to three days. Cells were monitored daily for death, comparing between positive and negative controls. Outgrowing colonies were picked and subcultured. No positive clones could be subcultured from the transfectants that received the mutant DHFR gene, most likely due to toxic effects of the high concentrations of MTX that were applied. From the PER.C6 and PER.C6/E2A cells that were transfected with the wild-type DHFR gene, only cell lines could be established in the first passages when cells were grown on 100 nM MTX, although colonies appeared on dishes with 250 and 500 nM MTX. These clones were not viable during subculturing, and were discarded.

Example 8

Sub-Culturing of Transfected Cells

From each cell line, approximately 50 selected colonies that were resistant to the threshold MTX concentration were grown subsequently in 96-well, 24-well, and 6-well plates and T25 flasks in their respective medium plus MTX. When cells reached growth in T25 tissue culture flasks, at least one vial of each clone was frozen and stored, and was subsequently tested for human recombinant EPO production. For this, the commercial ELISA kit from R&D Systems was used (Quantikine IVD human EPO, Quantitative Colorimetric Sandwich ELISA, cat.# DEPOO). Since the different clones appeared to have different growth characteristics and growth curves, a standard for EPO production was set as follows: At day 0, cells were seeded in T25 tissue culture flasks in concentrations ranging between 0.5 to 1.5 million per flask. At day 4, supernatant was taken and used in the EPO ELISA. From this, the production level was set as ELISA units per million seeded cells per day. (U/1E6/day) A number of these clones are given in Table 2 of the incorporated '007 patent application.

The following selection of good producer clones was based on high expression, culturing behavior and viability. To allow checks for long-term viability, suspension growth in roller bottles and bioreactor during extended time periods, more vials of the best producer clones were frozen, and the following best producers of each cell line were selected for further investigations P8, P9, E17 and E55 in which “P” stands for PER.C6 and “E” stands for PER.C6/E2A. These clones are subcultured and subjected to increasing doses of methotrexate in a time span of two months. The concentration starts at the threshold concentration and increases to approximately 0.2 mM. During these two months, EPO ELISA experiments are performed on a regular basis to detect an increase in EPO production. At the highest methotrexate concentration, the best stable producer is selected and compared to the amounts from the best CHO clone and used for cell banking (RL). From every other clone, five vials are frozen. The number of amplified EPO cDNA copies is detected by Southern blotting.

Example 9

EPO Production in Bioreactors

The best performing EPO producing transfected stable cell line of PER.C6, P9, was brought into suspension and scaled up to 1 to 2 liter fermentors. To get P9 into suspension, attached cells were washed with PBS and subsequently incubated with JRH ExCell 525 medium for PER.C6 (JRH Biosciences), after which the cells loosen from the flask and form the suspension culture. Cells were kept at two concentrations of MTX: 0 nM and 100 nM. General production levels of EPO that were reached at these concentrations (in roller bottles) were respectively 1500 and 5700 units per million seeded cells per day. Although the lower yields in the absence of MTX can be explained by removal of the integrated DNA, it seems as if there is a shut-down effect of the integrated DNA since cells that are kept at lower concentrations of MTX for longer periods of time are able to reach their former yields when they are transferred to 100 nM MTX concentrations again. (See, Example 11.)

Suspension P9 cells were grown normally with 100 nM MTX and used for inoculation of bioreactors. Two bioreactor settings were tested: perfusion and repeated batch cultures.

A. Perfusion in a 2 Liter Bioreactor.

Cells were seeded at a concentration of 0.5×10⁶ cells per ml and perfusion was started at day 3 after cells reached a density of approximately 2.3×10⁶ cells per ml. The perfusion rate was 1 volume per 24 hours with a bleed of approximately 250 ml per 24 hours. In this setting, P9 cells stayed at a constant density of approximately 5×10⁶ cells per ml and a viability of almost 95% for over a month. The EPO concentration was determined on a regular basis and is shown in FIG. 15 (of the incorporated '007 application). In the 2 liter perfused bioreactor the P9 cells were able to maintain a production level of approximately 6000 ELISA units per ml. With a perfusion rate of one working volume per day (1.5 to 1.6 liter), this means that in this 2 liter setting, the P9 cells produced approximately 1×10⁷ units per day per 2 liter bioreactor in the absence of MTX.

B. Repeated Batch in a 2 Liter Bioreactor.

P9 suspension cells that were grown on roller bottles were used to inoculate a 2 liter bioreactor in the absence of MTX and were left to grow until a density of approximately 1.5 million cells per ml, after which a third of the population was removed (+/−1 liter per 2 to 3 days) and the remaining culture was diluted with fresh medium to reach again a density of 0.5 million cells per ml. This procedure was repeated for three weeks and the working volume was kept at 1.6 liter. EPO concentrations in the removed medium were determined and shown in FIG. 16 of the incorporated '007 application. The average concentration was approximately 3000 ELISA units per ml. With an average period of two days after which the population was diluted, this means that, in this 2 liter setting, the P9 cells produced approximately 1.5×10⁶ units per day in the absence of MTX.

C. Repeated Batch in a 1 Liter Bioreactor with Different Concentrations of Dissolved Oxygen, Temperatures and pH Settings.

Fresh P9 suspension cells were grown in the presence of 100 nM MTX in roller bottles and used for inoculation of 4×1 liter bioreactors to a density of 0.3 million cells per ml in JRH ExCell 525 medium. EPO yields were determined after 3, 5 and 7 days. The first settings that were tested were: 0.5%, 10%, 150% and as a positive control 50% Dissolved Oxygen (% DO). 50% DO is the condition in which PER.C6 and P9 cells are normally kept. In another run, P9 cells were inoculated and tested for EPO production at different temperatures (32° C., 34° C., 37° C. and 39° C.) in which 37° C. is the normal setting for PER.C6 and P9, and in the third run, fresh P9 cells were inoculated and tested for EPO production at different pH settings (pH 6.5, pH 6.8, pH 7.0 and pH 7.3). PER.C6 cells are normally kept at pH 7.3. An overview of the EPO yields (three days after seeding) is shown in FIG. 17 of the incorporated '007 application. Apparently, EPO concentrations increase when the temperature is rising from 32 to 39° C. as was also seen with PER.C6/E2A cells grown at 39° C. (Table 4) (of the incorporated '007 application), and 50% DO is optimal for P9 in the range that was tested here. At pH 6.5, cells cannot survive since the viability in this bioreactor dropped beneath 80% after seven days. EPO samples produced in these settings are checked for glycosylation and charge in 2D electrophoresis. (See, also Example 17.)

Example 10

Amplification of the DHFR Gene

A number of cell lines described in Example 8 were used in an amplification experiment to determine the possibility of increasing the number of DHFR genes by increasing the concentration of MTX in a time span of more than two months. The concentration started at the threshold concentration (100 nM) and increased to 1800 nM with in-between steps of 200 nM, 400 nM, 800 nM and 1200 nM. During this period, EPO ELISA experiments were performed on a regular basis to detect the units per million seeded cells per day (FIG. 18 of the incorporated '007 application). At the highest MTX concentration (1800 nM), some vials were frozen. Cell pellets were obtained and DNA was extracted and subsequently digested with BglII, since this enzyme cuts around the wild-type DHFR gene in pEPO2000/DHFRwt (FIG. 5 of the incorporated '007 application), so a distinct DHFR band of that size would be distinguishable from the endogenous DHFR bands in a Southern blot. This DNA was run and blotted and the blot was hybridized with a radioactive DHFR probe and subsequently with an adenovirus E1 probe as a background control (FIG. 19 of the incorporated '007 application). The intensities of the hybridizing bands were measured in a phosphorimager and corrected for background levels. These results are shown in Table 3 of the incorporated '007 application. Apparently, it is possible to obtain amplification of the DHFR gene in PER.C6 cells, albeit in this case only with the endogenous DHFR and not with the integrated vector.

Example 11

Stability of EPO Expression in Stable Cell Lines

A number of cell lines mentioned in Example 8 were subject to long term culturing in the presence and absence of MTX. EPO concentrations were measured regularly in which 1.0 to 1.5×10⁶ cells per T25 flask were seeded and left for four days to calculate the production levels of EPO per million seeded cells per day. The results are shown in FIG. 20 of the incorporated '007 application. From this, it is concluded that there is a relatively stable expression of EPO in P9 cells when cells are cultured in the presence of MTX and that there is a decrease in EPO production in the absence of MTX. However, when P9 cells were placed on 100 nM MTX again after being cultured for a longer period of time without MTX, the expressed EPO reached its original level (+/−3000 ELISA units per million seeded cells per day), suggesting that the integrated plasmids are shut off but are stably integrated and can be switched back on again. It seems as if there are differences between the cell lines P8 and P9 because the production level of P8 in the presence of MTX is decreasing in time over a high number of passages (FIG. 20A of the incorporated '007 application), while P9 production is stable for at least 62 passages (FIG. 20B of the incorporated '007 application).

Example 12

Transient Expression of Recombinant EPO on Attached and Suspension Cells after Plasmid DNA Transfections

pEPO2000/DHFRwt, pEPO2000/DHFRm and pAdApt.EPO plasmids from Example 2 are purified from E. coli over columns, and are transfected using lipofectamine, electroporation, PEI or other methods. PER.C6 or PER.C6/E2A cells are counted and seeded in DMEM plus serum or JRH ExCell 525 medium or the appropriate medium for transfection in suspension. Transfection is performed at 37° C. up to 16 hours, depending on the transfection method used, according to procedures known by a person skilled in the art. Subsequently, the cells are placed at different temperatures and the medium is replaced by fresh medium with or without serum. In the case when it is necessary to obtain medium that completely lacks serum components, the fresh medium lacking serum is removed again after 3 hours and replaced again by medium lacking serum components. For determination of recombinant EPO production, samples are taken at different time points. Yields of recombinant protein are determined using an ELISA kit (R&D Systems) in which 1 Unit equals approximately 10 ng of recombinant CHO-produced EPO protein (100,000 Units/mg). The cells used in these experiments grow at different rates, due to their origin, characteristics and temperature. Therefore, the amount of recombinant EPO produced is generally calculated in ELISA units/10⁶ seeded cells/day, taking into account that the antisera used in the ELISA kit do not discriminate between non- and highly glycosylated recombinant EPO. Generally, samples for these calculations are taken at day 4 after replacing the medium upon transfection.

PER.C6/E2A cells, transfected at 37° C. using lipofectamine and subsequently grown at 39° C. in the presence of serum, typically produced 3100 units/10⁶ cells/day. In the absence of serum components without any refreshment of medium lacking serum, these lipofectamine-transfected cells typically produced 2600 units/10⁶ cells/day. PER.C6 cells, transfected at 37° C. using lipofectamine and subsequently grown at 37° C. in the presence of serum, typically produced 750 units/10⁶ cells/day and, in the absence of serum, 590 units/10⁶ cells/day. For comparison, the same expression plasmids pEPO2000/DHFRwt and pEPO2000/DHFRm were also applied to transfect CHO cells (ECACC deposit no. 85050302) using lipofectamine, PEI, calcium phosphate procedures and other methods. When CHO cells were transfected using lipofectamine and subsequently cultured in Hams F12 medium in the presence of serum, a yield of 190 units/10⁶ cells/day was obtained. In the absence of serum, 90 units/10⁶ cells/day were produced, although higher yields can be obtained when transfections are being performed in DMEM.

Different plates containing attached PER.C6/E2A cells were also transfected at 37° C. with pEPO2000/DHFRwt plasmid and subsequently placed at 32° C., 34° C., 37° C. or 39° C. to determine the influence of temperature on recombinant EPO production. A temperature-dependent production level was observed ranging from 250 to 610 units/10⁶ seeded cells/day, calculated from a day 4 sample, suggesting that the difference between production levels observed in PER.C6 and PER.C6/E2A is partly due to incubation temperatures (see, also FIG. 17 of the incorporated '007 application). Since PER.C6/E2A grows well at 37° C., further studies were performed at 37° C.

Different plates containing attached PER.C6 and PER.C6/E2A cells were transfected with pEPO2000/DHFRwt, pEPO2000/DHFRm and pAdApt.EPO using lipofectamine. Four hours after transfection, the DMEM was replaced with either DMEM plus serum or JRH medium lacking serum and EPO was allowed to accumulate in the supernatant for several days to determine the concentrations that are produced in the different mediums. PER.C6 cells were incubated at 37° C., while PER.C6/E2A cells were kept at 39° C. Data from the different plasmids were averaged since they contain a similar expression cassette. Calculated from a day 6 sample, the following data were obtained: PER.C6 grown in DMEM produced 400 units/10⁶ seeded cells/day, and when they were kept in JRH medium, they produced 300 units/10⁶ seeded cells/day. PER.C6/E2A grown in DMEM produced 1800 units/10⁶ seeded cells/day, and when they were kept in JRH, they produced 1100 units/10⁶ seeded cells/day. Again, a clear difference was observed in production levels between PER.C6 and PER.C6/E2A, although this might partly be due to temperature differences. There was, however, a significant difference with PER.C6/E2A cells between the concentration in DMEM vs. the concentration in JRH medium, although this effect was almost completely lost in PER.C6 cells.

EPO expression data obtained in this system are summarized in Table 4 (of the incorporated '007 application). PER.C6 and derivatives thereof can be used for scaling up the DNA transfections system. According to Wurm and Bernard (1999), transfections on suspension cells can be performed at 1 to 10 liter set-ups in which yields of 1 to 10 mg/l (0.1 to 1 pg/cell/day) of recombinant protein have been obtained using electroporation. A need exists for a system in which this can be well controlled and yields might be higher, especially for screening of large numbers of proteins and toxic proteins that cannot be produced in a stable setting. With the lipofectamine transfections on the best PER.C6 cells in the absence of serum, we reached 590 units/million cells/day (+/−5.9 pg/cell/day when 1 ELISA unit is approximately 10 ng EPO), while PER.C6/E2A reached 31 pg/cell/day (in the presence of serum). The medium used for suspension cultures of PER.C6 and PER.C6/E2A (JRH ExCell 525) does not support efficient transient DNA transfections using components like PEI. Therefore, the medium is adjusted to enable production of recombinant EPO after transfection of pEPO2000/DHFRwt and pEPO2000/DHFRm containing a recombinant human EPO cDNA, and pcDNA2000/DHFRwt containing other cDNAs encoding recombinant proteins.

One to 10 liter suspension cultures of PER.C6 and PER.C6/E2A growing in adjusted medium to support transient DNA transfections using purified plasmid DNA are used for electroporation or other methods, performing transfection with the same expression plasmids. After several hours, the transfection medium is removed and replaced by fresh medium without serum. The recombinant protein is allowed to accumulate in the supernatant for several days, after which the supernatant is harvested and all the cells are removed. The supernatant is used for down stream processing to purify the recombinant protein.

Example 13

Generation of AdApt.EPO Recombinant Adenoviruses

pAdApt.EPO was co-transfected with the pWE/Ad.AflII-rITR.tetO-E4, pWE/Ad.AflII-rITR.DE2A, and pWE/Ad.AflII-rITR.DE2A.tetO-E4 cosmids in the appropriate cell lines using procedures known to persons skilled in the art. Subsequently, cells were left at their appropriate temperatures for several days until full cytopathic effect (“CPE”) was observed. Then cells were applied to several freeze/thaw steps to free all viruses from the cells, after which the cell debris was spun down. For IG.Ad5/AdApt.EPO.dE2A, the supernatant was used to infect cells, followed by an agarose overlay for plaque purification using several dilutions. After a number of days, when single plaques were clearly visible in the highest dilutions, nine plaques and one negative control (picked cells between clear plaques, so most likely not containing virus) were picked and checked for EPO production on A549 cells. All plaque picked viruses were positive and the negative control did not produce recombinant EPO. One positive producer was used to infect the appropriate cells and to propagate virus starting from a T-25 flask to a roller bottle setting. Supernatants from the roller bottles were used to purify the virus, after which the number of virus particles (vps) was determined and compared to the number of infectious units (IUs) using procedures known to persons skilled in the art. Then, the vp/IU ratio was determined.

Example 14

Infection of Attached and Suspension PER.C6 Cells with IG.Ad5/AdApt.EPO.dE2A

Purified viruses from Example 13 were used for transient expression of recombinant EPO in PER.C6 cells and derivatives thereof. IG.Ad5/AdApt.EPO.dE2A virus was used to infect PER.C6 cells, while IG.Ad5/AdApt.EPO.tetOE4 and IG.Ad5/AdApt.EPO.dE2A.tetOE4 viruses can be used to infect PER.C6/E2A cells to lower the possibility of replication and, moreover, to prevent inhibition of recombinant protein production due to replication processes. Infections were performed on attached cells as well as on suspension cells in their appropriate medium using ranges of multiplicities of infection (moi's): 20, 200, 2000, 20000 vp/cell. Infections were performed for four hours in different settings ranging from six-well plates to roller bottles, after which the virus containing supernatant was removed. The cells were washed with PBS or directly refreshed with new medium. Then, cells were allowed to produce recombinant EPO for several days, during which samples were taken and EPO yields were determined. Also, the number of viable cells compared to dead cells was checked. The amount of EPO that was produced was again calculated as ELISA unit seeded cells/day, because the different cell lines have different growth characteristics due to their passage number and environmental circumstances such as temperature and selective pressures. Suspension growing PER.C6 cells were seeded in 250 ml JRH ExCell 525 medium in roller bottles (1 million cells per ml) and subsequently infected with purified IG.Ad5/AdApt.EPO.dE2A virus with a moi of 200 vp/cell. The estimation used for vp determination was high (vp/tU ratio of this batch is 330, which indicates an moi of 0.61 IUs/cell). Thus, not all cells were hit by an infectious virus. A typical production of recombinant EPO in this setting from a day 6 sample was 190 units/10⁶ seeded cells/day, while in a setting in which 50% of the medium including viable and dead cells was replaced by fresh medium, approximately 240 units/10⁶ cells/day were obtained. The refreshment did not influence the viability of the viable cells, but the removed recombinant protein could be added to the amount that was obtained at the end of the experiment, albeit present in a larger volume. An identical experiment was performed with the exception that cells were infected with a moi of 20 vp/cell, resembling approximately 0.06 Infectious Units/cell. Without refreshment, a yield of 70 ELISA units/I 06 cells/day was obtained, while in the experiment in which 50% of the medium was refreshed at day 3, a typical amount of 80 units/10⁶ cells/day was measured. This indicates that there is a dose response effect when an increasing number of infectious units are used for infection of PER.C6 cells.

Furthermore, PER.C6 cells growing in DMEM were seeded in six-well plates and left overnight in 2 ml DMEM with serum to attach. The next day, cells were infected with another batch of IG.Ad5/AdApt.EPO.dE2A virus (vp/IU ratio 560) with a moi of 200 vp/cells (0.35 Infectious Units/cell). After four hours, the virus containing medium was removed and replaced by fresh medium including serum, and cells were left to produce recombinant EPO for more than two weeks with replacement of the medium with fresh medium every day. The yield of recombinant EPO production calculated from a day 4 sample was 60 units/10⁶ cells/day.

Expression data obtained in this system have been summarized in Table 5 (of the incorporated '007 application).

Due to the fact that a tTA-tetO regulated expression of the Early region 4 of adenovirus (E4) impairs the replication capacity of the recombinant virus in the absence of active E4, it is also possible to use the possible protein production potential of the PER.C6/E2A as well as its parental cell line PER.C6 to produce recombinant proteins in a setting in which a recombinant adenovirus is carrying the human EPO cDNA as the transgene and in which the E4 gene is under the control of a tet operon. Then, very low levels of E4 mRNA are being produced, resulting in very low but detectable levels of recombinant and replicating virus in the cell line PER.C6/E2A and no detectable levels of this virus in PER.C6 cells. To produce recombinant EPO in this way, the two viruses IG.Ad5/AdApt.EPO.tetOE4 and IG.Ad5/AdApt.EPO.dE2A.tetOE4 are used to infect PER.C6 cells and derivatives thereof. Attached and suspension cells are infected with different moi's of the purified adenoviruses in small settings (six-well plates and T25 flasks) and large settings (roller bottles and fermentors). Samples are taken at different time points and EPO levels are determined.

Since viruses that are deleted in E1 and E2A in the viral backbone can be complemented in PER.C6/E2A cells but not in the original PER.C6 cells, settings are used in which a mixture of both cell lines is cultured in the presence of IG.Ad5/AdApt.EPO.dE2A virus. The virus will replicate in PER.C6/E2A, followed by lysis of the infected cells and a subsequent infection of PER.C6 or PER.C6/E2A cells. In contrast, in PER.C6 cells, the virus will not replicate and the cells will not lyse due to viral particle production, but will produce recombinant EPO that will be secreted in the supernatant. A steady state culture/replication/EPO production system is set up in which fresh medium and fresh PER.C6 and PER.C6/E2A cells are added at a constant flow, while used medium, dead cells and debris are removed. Together with this, recombinant EPO is taken from the system and used for purification in a down stream processing procedure in which virus particles are removed.

Example 15

Purification and Analysis of Recombinant EPO

Large batches of growing cells are produced in bioreactors; the secreted recombinant human EPO protein is purified according to procedures known by one of skill in the art. The purified recombinant human EPO protein from PER.C6 and PER.C6/E2A stable clones or transfectants is checked for glycosylation and folding by comparison with commercially available EPO and EPO purified from human origin (urine) using methods known to one of skill in the art (see, Examples 16 and 17). Purified and glycosylated EPO proteins from PER.C6 and PER.C6/E2A are tested for biological activity in in vitro experiments and in mouse spleens as described (Krystal (1983) and in vitro assays (see, Example 18).

Example 16

Activity of Beta-galactoside Alpha 2,6-sialyltransferase in PER.C6

It is known that CHO cells do not contain a gene for beta-galactoside alpha 2,6-sialyltransferase, resulting in the absence of alpha 2,6-linked sialic acids at the terminal ends of—and O-linked oligosaccharides of endogenous and recombinant glycoproteins produced on these CHO cells. Since the alpha 2,3-sialyltransferase gene is present in CHO cells, proteins that are produced on these cells are typically from the 2,3 linkage type. EPO that was purified from human urine does, however, contain both alpha 2,3- and alpha 2,6-linked sialic acids. To determine whether PER.C6 cells, being a human cell line, are able to produce recombinant EPO containing both alpha 2,3- and alpha 2,6-linkages, a direct neuraminidase assay was performed on recombinant EPO produced on PER.C6 cells after transfection with EPO expression vectors. As a control, commercially available Eprex samples were used, which were derived from CHO cells and which should only contain sialic acid linkages of the alpha 2,3 type. The neuraminidases that were used were from Newcastle Disease Virus (NDV) that specifically cleaves alpha 2,3-linked neuraminic acids (sialic acids) from—and O-linked glycans, and from Vibrocholerae (VC) that non-specifically cleaves all terminal—or O-linked sialic acids (alpha 2,3, alpha 2,6 and alpha 2,8 linkages). Both neuraminidases were from Boehringer and were incubated with the samples according to guidelines provided by the manufacturer. Results are shown in FIG. 21A (of the incorporated '007 application). In lanes 2 and 3 (treatment with NDV neuraminidase), a slight shift is observed as compared to lane 1 (non-treated PER.C6 EPO). When this EPO sample was incubated with VC derived neuraminidase, an even faster migrating band is observed as compared to NDV treated samples. However, with the commercially available Eprex, only a shift was observed when NDV derived neuraminidase was applied (lanes 6 and 7 compared to the non-treated sample in lane 5) and not when VC neuraminidase was used (lane 8).

To definitely establish that no sialic acids of the alpha 2,6 linkage type are present on CHO cells, but that they do exist in proteins present on the cell surface of PER.C6 cells, the following experiment was performed: CHO cells were released from the solid support using trypsin-EDTA, while for PER.C6, suspension cells were used. Both suspensions were washed once with Mem-5% FBS and incubated in this medium for one hour at 37° C. After washing with PBS, the cells were resuspended to approximately 10⁶ cells/ml in binding medium (Tris-buffered saline, pH 7.5, 0.5% BSA, and 1 mM each of MgCl₂, MnCl₂ and CaCl₂). Aliquots of the cells were incubated for 1 hour at room temperature with DIG-labeled lectins, Sambucus nigra agglutinin (“SNA”) and Maackia amurensis agglutinin (“MAA”), which specifically bind to sialic acid linkages of the alpha 2,6 Gal and alpha 2,3 Gal types, respectively. Control cells were incubated without lectins. After one hour, both lectin-treated and control cells were washed with PBS and then incubated for one hour at room temperature with FITC-labeled anti-DIG antibody (Boehringer-Mannheim). Subsequently, the cells were washed with PBS and analyzed for fluorescence intensity on a FACsort apparatus (Becton Dickinson). The FACS analysis is shown in FIG. 21B (of the incorporated '007 application). When the SNA lectin is incubated with CHO cells, no shift is seen as compared to non-treated cells, while when this lectin is incubated with PER.C6 cells, a clear shift (dark fields) is observed as compared to non-treated cells (open fields). When both cell lines are incubated with the MAA lectin, both cell lines give a clear shift as compared to non-treated cells.

From these EPO digestions and FACS results, it is concluded that there is a beta-galactoside alpha 2,6 sialyltransferase activity present in human PER.C6 cells which is absent in CHO cells.

Example 17

Determination of Sialic Acid Content in PER.C6 Produced EPO

The terminal neuraminic acids (or sialic acids) that are present on the—and O-linked glycans of EPO protect the protein from clearance from the bloodstream by enzymes in the liver. Moreover, since these sialic acids are negatively charged, one can distinguish between different EPO forms depending on their charge or specific pI. Therefore, EPO produced on PER.C6 and CHO cells was used in two-dimensional electrophoresis in which the first dimension separates the protein on charge (pH range 3-10) and the second dimension separates the proteins further on molecular weight. Subsequently, the proteins were blotted and detected in a western blot with an anti-EPO antibody.

It is also possible to detect the separated EPO protein by staining the gel using Coomassie blue or silver staining methods, subsequently removing different spots from the gel and determining the specific glycan composition of the different—or O-linked glycosylations that are present on the protein by mass spectrometry.

In FIG. 22A of the incorporated '007 application, a number of EPO samples are shown that were derived from P9 supernatants. P9 is the PER.C6 cell line that stably expresses recombinant human EPO (see, Example 8). These samples were compared to commercially available Eprex, which contains only EPO forms harboring approximately 9 to 14 sialic acids. Eprex should, therefore, be negatively charged and be focusing towards the pH3 side of the gel. FIG. 22B (of the incorporated '007 application) shows a comparison between EPO derived from P9 in an attached setting in which the cells were cultured on DMEM medium and EPO derived from CHO cells that were transiently transfected with the pEPO2000/DHFRwt vector. Apparently, the lower forms of EPO cannot be detected in the CHO samples, whereas all forms can be seen in the P9 sample. The sialic acid content is given by numbering the bands that were separated in the first dimension from 1 to 14. It is not possible to determine the percentage of each form of EPO molecules present in the mixtures because the western blot was performed using ECL, and because it is unknown whether glycosylation of the EPO molecule or transfer of the EPO molecule to the nitrocellulose inhibits recognition of the EPO molecule by the antibody. However, it is possible to determine the presence of the separate forms of sialic acid containing EPO molecules. It can be concluded that PER.C6 is able to produce the entire range of 14 sialic acid containing isoforms of recombinant human EPO.

Example 18

In vitro Functionality of PER.C6 Produced EPO

The function of recombinant EPO in vivo is determined by its half-life in the bloodstream. Removal of EPO takes place by liver enzymes that bind to galactose residues in the glycans that are not protected by sialic acids and by removal through the kidney. Whether this filtering by the kidney is due to misfolding or due to under- or mis-glycosylation is unknown. Furthermore, EPO molecules that reach their targets in the bone marrow and bind to the EPO receptor on progenitor cells are also removed from circulation. Binding to the EPO receptor and down stream signaling depends heavily on a proper glycosylation status of the EPO molecule. Sialic acids can, to some extent, inhibit binding of EPO to the EPO receptor, resulting in a lower effectiveness of the protein. However, since the sialic acids prevent EPO from removal, these sugars are essential for its function to protect the protein on its travel to the EPO receptor. When sialic acids are removed from EPO in vitro, a better binding to the receptor occurs, resulting in a stronger down stream signaling. This means that the functionalities in vivo and in vitro are significantly different, although a proper EPO receptor binding property can be checked in vitro despite the possibility of an under-sialylation causing a short half-life in vivo (Takeuchi et al., 1989).

Several in vitro assays for EPO functionality have been described of which the stimulation of the IL3, GM-CSF and EPO-dependent human cell line TF-1 is most commonly used. Hereby, one can determine the number of in vitro units per mg (Kitamura et al., 1989; Hammerling et al., 1996). Other in vitro assays are the formation of red colonies under an agarose layer of bone marrow cells that were stimulated to differentiate by EPO, the incorporation of 59Fe into heme in cultured mouse bone marrow cells (Krystal et al., 1981 and 1983; Takeuchi et al., 1989), in rat bone marrow cells (Goldwasser et al., 1975) and the Radio Immuno Assay (RIA) in which the recognition of EPO for antisera is determined.

EPO produced on PER.C6/E2A cells was used to stimulate TF-1 cells as follows: Cells were seeded in 96-well plates with a density of around 10,000 cells per well in medium lacking IL3 or GM-CSF, which are the growth factors that can stimulate indefinite growth of these cells in culture. Subsequently, medium is added, resulting in final concentrations of 0.0001, 0.001, 0.01, 0.1, 1 and 10 units per ml. These units were determined by ELISA, while the units of the positive control Eprex were known (4000 units per ml) and were diluted to the same concentration. Cells were incubated with these EPO samples for four days, after which an MTS assay (Promega) was performed to check for viable cells by fluorescence measurement at 490 nm (fluorescence is detectable after transfer of MTS into formazan). FIG. 23 of the incorporated '007 application shows the activity of two samples derived from PER.C6/E2A cells that were transfected with an EPO expression vector and subsequently incubated at 37° C. and 39° C. for four days. The results suggest that samples obtained at 39° C. are more active than samples obtained at 37° C., which might indicate that the sialic acid content is suboptimal at higher temperatures. It is hereby shown that PER.C6 produced EPO can stimulate TF-1 cells in an in vitro assay, strongly suggesting that the EPO that is produced on this human cell line can interact with the EPO receptor and stimulate differentiation.

Example 19

Production of Recombinant Murine, Humanized and Human Monoclonal Antibodies in PER.C6 and PER.C6/E2A

A. Transient DNA Transfections

cDNAs encoding heavy and light chains of murine, humanized and human monoclonal antibodies (mAbs) are cloned in two different systems: one in which the heavy and light chains are integrated into one single plasmid (a modified pcDNA2000/DHFRwt plasmid) and the other in which heavy and light chain cDNAs are cloned separately into two different plasmids (see, Examples 1, 3, 4 and 5). These plasmids can carry the same selection marker (like DHFR) or they carry their own selection marker (one that contains the DHFR gene and one that contains, for instance, the neo-resistance marker). For transient expression systems, it does not matter what selection markers are present in the backbone of the vector since no subsequent selection is being performed. In the common and regular transfection methods used in the art, equal amounts of plasmids are transfected. A disadvantage of integrating both heavy and light chains on one single plasmid is that the promoters that are driving the expression of both cDNAs might influence each other, resulting in non-equal expression levels of both subunits, although the number of cDNA copies of each gene is exactly the same.

Plasmids containing the cDNAs of the heavy and light chain of a murine and a humanized monoclonal antibody are transfected and, after several days, the concentration of correctly folded antibody is determined using methods known to persons skilled in the art. Conditions such as temperature and used medium are checked for both PER.C6 and PER.C6/E2A cells. Functionality of the produced recombinant antibody is controlled by determination of affinity for the specified antigen.

B. Transient Viral Infections

cDNAs encoding a heavy and a light chain are cloned in two different systems: one in which the heavy and light chains are integrated into one single adapter plasmid (a modified pAdApt.pac) and the other in which heavy and light chain cDNAs are cloned separately into two different adapters (each separately in pAdApt.pac). In the first system, viruses are propagated that carry an E1 deletion (dE1) together with an E2A deletion (dE2A) or both deletions in the context of a tetOE4 insertion in the adenoviral backbone. In the second system, the heavy and light chains are cloned separately in pAdApt.pac and separately propagated to viruses with the same adenoviral backbone. These viruses are used to perform single or co-infections on attached and suspension growing PER.C6 and PER.C6/E2A cells. After several days, samples are taken to determine the concentration of full length recombinant antibodies, after which the functionality of these antibodies is determined using the specified antigen in affinity studies.

C. Stable Production and Amplification of the Integrated Plasmid.

Expression plasmids carrying the heavy and light chain together and plasmids carrying the heavy and light chain separately are used to transfect attached PER.C6 and PER.C6/E2A and CHO-dhfr cells. Subsequently, cells are exposed to MTX and/or hygromycin and neomycin to select for integration of the different plasmids. Moreover, a double selection with G418 and hygromycin is performed to select for integration of plasmids that carry the neomycin and hygromycin resistance gene. Expression of functional full length monoclonal antibodies is determined and best expressing clones are used for subsequent studies including stability of integration, copy number detection, determination of levels of both subunits and ability to amplify upon increase of MTX concentration after the best performing cell lines are used for mAb production in larger settings such as perfused and (fed-) batch bioreactors, after which optimization of quantity and quality of the mAbs is executed.

Example 20

Transfection of mAb Expression Vectors to Obtain Stable Cell Lines

PER.C6 cells were seeded in DMEM plus 10% FBS in 47-tissue culture dishes (10 cm diameter) with approximately 2.5×10⁶ cells per dish and were kept overnight under their normal culture conditions (10% CO₂ concentration and 37° C.). The next day, co-transfections were performed in 39 dishes at 37° C. using Lipofectamine in standard protocols with 1 μg MunI-digested and purified pUBS-Heavy2000/Hyg(−) and 1 μg Seal-digested and purified pUBS-Light2001/Neo (see, Example 3) per dish, while two dishes were co-transfected as controls with 1 μg MunI-digested and purified pcDNA2000/Hyg(−) and 1 μg Seal-digested and purified pcDNA2001/Neo. As a control for transfection efficiency, four dishes were transfected with a LacZ control vector, while two dishes were not transfected and served as negative controls.

After hours, cells were washed twice with DMEM and re-fed with fresh medium without selection. The next day, medium was replaced by fresh medium containing different selection reagents: 33 dishes of the heavy and light chain co-transfectants, two dishes that were transfected with the empty vectors and the two negative controls (no transfection) were incubated only with 50 μg per ml hygromycin, two dishes of the heavy and light chain co-transfectants and two dishes of the transfection efficiency dishes (LacZ vector) were incubated only with 500 μg per ml G418, while two transfection efficiency dishes were not treated with selection medium but used for transfection efficiency that was around 40%. Two dishes were incubated with a combination of 50 μg per ml hygromycin and 250 μg per ml G418 and two dishes were incubated with 25 μg per ml hygromycin and 500 μg per ml G418.

Since cells were overgrowing when they were only incubated with hygromycin alone, it was decided that a combination of hygromycin and G418 selection would immediately kill the cells that integrated only one type of the two vectors that were transfected. Seven days after seeding, all co-transfectants were further incubated with a combination of 100 μg per ml hygromycin and 500 μg per ml G418. Cells were refreshed two or three days with medium containing the same concentrations of selecting agents. Fourteen days after seeding, the concentrations were adjusted to 250 μg per ml G418 and 50 μg per ml hygromycin. Twenty-two days after seeding, a large number of colonies had grown to an extent in which it was possible to select, pick and subculture. Approximately 300 separate colonies were selected and picked from the 10 cm dishes and subsequently grown via 96 wells and/or 24 wells via six-well plates to T25 flasks. In this stage, cells are frozen (four vials per subcultured colony) and production levels of recombinant UBS-54 mAb are determined in the supernatant using the ELISA described in Example 26.

CHO-dhfr cells are seeded in DMEM plus 10% FBS including hypoxanthine and thymidine in tissue culture dishes (10 cm diameter) with approximately 1 million cells per dish and are kept overnight under normal conditions and used for a co-transfection the next day with pUBS-Heavy2000/Hyg(−) and pUBS-Light2001/DHFRwt under standard protocols using Lipofectamine. Medium is replaced with fresh medium after a few hours and split to different densities to allow the cells to adjust to the selection medium when stable integration is taking place without a possible outgrowth of non-transfected cells. Colonies are first selected on hygromycin resistance and, subsequently, MTX is added to select for double integrations of the 2 plasmids in these subcultured cell lines.

Transfections as described for pUBS-Heavy2000/Hyg(−) and pUBS-Light2001/Neo are performed with pUBS2-Heavy2000/Hyg(−) and pUBS2-Light2001/Neo in PER.C6 and PER.C6/E2A and selection is performed with either subsequent incubation with hygromycin followed by G418 or as described above with a combination of both selection reagents. CHO-dhfr cells are transfected with pUBS2-Heavy2000/Hyg(−) and pUBS2-Light2001/DHFRwt as described herein and selection is performed in a sequential way in which cells are first selected with hygromycin, after which an integration of the light chain vector is controlled by selection on MTX.

Furthermore, PER.C6 and PER.C6/E2A cells are also used for transfections with pUBS-3000/Hyg(−) and pUBS2-3000/Hyg(−), while CHO-dhfr cells are transfected with pUBS-3000/DHFRwt and pUBS2-3000/DHFRwt, after which a selection and further amplification of the integrated plasmids are performed by increasing the MTX concentration. In the case of the pcDNAs3000 plasmids, an equal number of mRNAs of both the heavy and light chain is expected, while in the case of two separate vectors, it is unclear whether a correct equilibrium is achieved between the two subunits of the immunoglobulin.

Transfections are also being performed on PER.C6, PER.C6/E2A and CHO-dhfr with expression vectors described in Examples 4 and 5 to obtain stable cell lines that express the humanized IgG1 mAb CAMPATH-1H and the humanized IgG1 mAb 15C5 respectively.

Example 21

Sub-Culturing of Transfected Cells

From PER.C6 cells transfected with pUBS-Heavy2000/Hyg (−) and PUBS-Light2001/Neo, approximately 300 colonies that were growing in medium containing Hygromycin and G418 were generally grown subsequently in 96-well, 24-well and 6-well plates in their respective medium plus their respective selecting agents. Cells that were able to grow in 24-well plates were checked for mAb production by using the ELISA described in Example 26. If cells scored positively, at least one vial of each clone was frozen and stored, and cells were subsequently tested and subcultured. The selection of a good producer clone is based on high expression, culturing behavior and viability. To allow checks for long term viability, amplification of the integrated plasmids and suspension growth during extended time periods, best producer clones are frozen, of which a number of the best producers of each cell line are selected for further work. Similar experiments are being performed on CHO-dhfr cells transfected with different plasmids and PER.C6 and PER.C6/E2A cells that were transfected with other combinations of heavy and light chains and other combinations of selection markers.

Example 22

mAb Production in Bioreactors

The best UBS-54 producing transfected cell line of PER.C6 is brought into suspension by washing the cells in PBS and then culturing the cells in JRH ExCell 525 medium, first in small culture flasks and subsequently in roller bottles, and scaled up to 1 to 2 liter fermentors. Cells are kept on hygromycin and G418 selection until it is proven that integration of the vectors is stable over longer periods of time. This is done when cells are still in their attached phase or when cells are in suspension.

Suspension growing mAb producing PER.C6 cells are generally cultured with hygromycin and G418 and used for inoculation of bioreactors from roller bottles. Production yields, functionality and quality of the produced mAb is checked after growth of the cells in perfused bioreactors and in fed batch settings.

A. Perfusion in a 2 Liter Bioreactor.

Cells are seeded in suspension medium in the absence of selecting agents at a concentration of approximately 0.5×10⁶ cells per ml and perfusion is started after a number of days when cell density reaches approximately 2 to 3×10⁶ cells per ml. The perfusion rate is generally 1 volume per 24 hours with a bleed of approximately 250 ml per 24 hours. In this setting, cells stay normally at a constant density of approximately 5×10⁶ cells per ml and a viability of almost 95% for over a month. The mAb production levels are determined on a regular basis.

B. Fed Batch in a 2 Liter Bioreactor.

In an initial run, mAb producing PER.C6 suspension cells that are grown on roller bottles are used to inoculate a 2 liter bioreactor in the absence of selecting agents to a density of 0.3 to 0.5 million cells per ml in a working volume of 300 to 500 ml and are left to grow until the viability of the cell culture drops to 10%. As a culture lifetime standard, it is determined at what day after inoculation the viable cell density drops beneath 0.5 million cells per ml. Cells normally grow until a density of 2 to 3 million cells per ml, after which the medium components become limiting and the viability decreases. Furthermore, it is determined how much of the essential components, such as glucose and amino acids in the medium are being consumed by the cells. Next to that, it is determined what amino acids are being produced and what other products are accumulating in the culture. Depending on this, concentrated feeding samples are being produced that are added at regular time points to increase the culture lifetime and thereby increase the concentration of the mAb in the supernatant. In another setting, 10× concentrated medium samples are developed that are added to the cells at different time points and that also increase the viability of the cells for a longer period of time, finally resulting in a higher concentration of mAb in the supernatant.

Example 23

Transient Expression of Humanized Recombinant Monoclonal Antibodies

The correct combinations of the UBS-54 heavy and light chain genes containing vectors were used in transient transfection experiments in PER.C6 cells. For this, it is not important which selection marker is introduced in the plasmid backbone, because the expression lasts for a short period (two to three days). The transfection method is generally lipofectamine, although other cationic lipid compounds for efficient transfection can be used. Transient methods are extrapolated from T25 flasks settings to at least 10-liter bioreactors. Approximately 3.5 million PER.C6 and PER.C6/E2A cells were seeded at day 1 in a T25 flask. At day 2, cells were transfected with, at most, 8 μg plasmid DNA using lipofectamine and refreshed after two to four hours and left for two days. Then, the supernatant was harvested and antibody titers were measured in a quantitative ELISA for human IgG1 immunoglobulins (CLB, see also Example 26). Levels of total human antibody in this system are approximately 4.8 μg/million seeded cells for PER.C6 and 11.1 μg/million seeded cells for PER.C6/E2A. To determine how much of the produced antibody is of full size and built up from two heavy and two light chains, as well as the expression levels of the heavy and/or light chain alone and connected by disulfide bridges, control ELISAs recognizing the sub-units separately are developed. Different capturing and staining antibody combinations are used that all detect human(ized) IgG1 sub-units. Supernatants of PER.C6 transfectants (transfected with control vectors or pUBS-Heavy2000/Hyg(−) and pUBS-Light2001/DHFRwt) were checked for full sized mAb production (FIG. 24) (of the incorporated '007 application). Samples were treated with and without DTT, wherein one can distinguish between full sized mAb (non-reduced) and heavy and light chain separately (reduced). As expected, the heavy chain is only secreted when the light chain is co-expressed and most of the antibody is of full size.

Example 24

Scale-Up System for Transient Transfections

PER.C6 and derivatives thereof are used for scaling up the DNA transfections system. According to Wurm and Bernard (1999), transfections on suspension cells can be performed at 1 to 10 liter set-ups in which yields of 1 to 10 mg/l (0.1 to 1 pg/cell/day) of recombinant protein have been obtained using electroporation.

A need exists for a system in which this can be well controlled and yields might be higher, especially for screening of large numbers of proteins and toxic proteins that cannot be produced in a stable setting. Moreover, since cell lines such as CHO are heavily affected by apoptosis-inducing agents such as lipofectamine, the art teaches that there is a need for cells that are resistant to this. Since PER.C6 is hardly affected by transfection methods, it seems that PER.C6 and derivatives thereof are useful for these purposes. One to 50 liter suspension cultures of PER.C6 and PER.C6/E2A growing in adjusted medium to support transient DNA transfections using purified plasmid DNA are used for electroporation or other methods, performing transfection with the same expression plasmids. After several hours, the transfection medium is removed and replaced by fresh medium without serum. The recombinant protein is allowed to accumulate in the supernatant for several days, after which the supernatant is harvested and all the cells are removed. The supernatant is used for down stream processing to purify the recombinant protein.

Example 25

Scale Up System for Viral Infections

Heavy and light chain cDNAs of the antibodies described in Examples 3, 4 and 5 are cloned into recombinant adenoviral adapter plasmids separately and in combination. The combinations are made to ensure an equal expression level for both heavy and light chains of the antibody to be formed. When heavy and light chains are cloned separately, viruses are being produced and propagated separately, of which the infectability and the concentration of virus particles are determined and finally co-infected into PER.C6 and derivatives thereof to produce recombinant mAbs in the supernatant. Production of adapter vectors, recombinant adenoviruses and mAbs is as described for recombinant EPO (see, Examples 13 and 14).

Example 26

Development of an ELISA for Determination of Human mAbs

Greiner microlon plates # 655061 were coated with an anti-human IgG1 kappa monoclonal antibody (Pharmingen #M032196 0.5) with 100 μl per well in a concentration of 4 μg per ml in PBS. Incubation was performed overnight at 4° C. or for 90 minutes at 37° C. Then, wells were washed three times with 0.05% Tween/PBS (400 μl per well) and subsequently blocked with 100 μl 5% milk dissolved in 0.05% Tween/PBS per well for 30 minutes at 37° C. and then, the plate was washed three times with 400 μl 0.05% Tween/PBS per well. As a standard, a purified human IgG1 antibody was used (Sigma, #108H9265) diluted in 0.5% milk/0.05% Tween/PBS in dilutions ranging from 50 to 400 ng per ml. Per well, 100 μl of the standard was incubated for one hour at 37° C. Then, the plate was washed three times with 400 μl per well 0.05% Tween/PBS. As the second antibody, a biotin labeled mouse monoclonal anti-human IgG1 antibody was used (Pharmingen #M045741) in a concentration of 2 ng per ml. Per well, 100 μl of this antibody was added and incubated for one hour at 37° C. and the wells were washed three times with 400 μl 0.05% Tween/PBS.

Subsequently, conjugate was added: 100 μl per well of a 1:1000 dilution of Streptavidin-HRP solution (Pharmingen #M045975) and incubated for one hour at 37° C., and the plate was again washed three times with 400 μl per well with 0.05% Tween/PBS.

One ABTS tablet (Boehringer Mannheim #600191-01) was dissolved in 50 ml ABTS buffer (Boehringer Mannheim #60328501) and 100 μl of this solution was added to each well and incubated for one hour at RT or 37° C. Finally, the OD was measured at 405 nm. Supernatant samples from cells transfected with mAb encoding vectors were generally dissolved and diluted in 0.5% milk/0.05% Tween/PBS. If samples did not fit with the linear range of the standard curve, other dilutions were used.

Example 27

Production of Influenza HA and NA Proteins in a Human Cell for Recombinant Subunit Vaccines

cDNA sequences of genes encoding hemagluttinin (HA) and neuraminidase (NA) proteins of known and regularly appearing novel influenza virus strains are being determined and generated by PCR with primers for convenient cloning into pcDNA2000, pcDNA2001, pcDNA2002 and pcDNAs3000 vectors (see, Example 1). Subsequently, these resulting expression vectors are being transfected into PER.C6 and derivatives thereof for stable and transient expression of the recombinant proteins to result in the production of recombinant HA and NA proteins that are, therefore, produced in a complete standardized way with human cells under strict and well-defined conditions. Cells are allowed to accumulate these recombinant HA and NA proteins for a standard period of time. When the pcDNAs3000 vector is used, it is possible to clone both cDNAs simultaneously and have the cells produce both proteins at the same time. From separate or combined cultures, the proteins are being purified following standard techniques and final HA and NA titers are being determined and activities of the proteins are checked by persons skilled in the art. Then, the purified recombinant proteins are used for vaccination studies and finally used for large-scale vaccination purposes.

The HA1 fragment of the swine influenza virus A/swine/Oedenrode/7C/96 (Genbank accession number AF092053) was obtained by PCR using a forward primer with the following sequence: 5′ ATT GGC GCG CCA CCA TGA AGA CTA TCA TTG CTT TGA GCT AC 3′ (SEQ ID NO:30) corresponding to the incorporated '007 application, and with a reverse primer with the following sequence: 5′ GAT GCT AGC TCA TCT AGT TTG TTT TTC TGG TAT ATT CCG 3′ (SEQ ID NO:31) corresponding to the incorporated '007 application. The resulting 1.0 kb PCR product was digested with AscI and NheI restriction enzymes and ligated with AscI and NheI-digested and purified pcDNA2000/DHFRwt vector, resulting in pcDNA2001/DHFRwt-swHA1. Moreover, the HA2 fragment of the same virus was amplified by PCR using the same forward primer as described for HA1 and another reverse primer with the following sequence: 5′ GAT GCT AGC TCA GTC TTT GTA TCC TGA CTT CAG TTC AAC ACC 3′ (SEQ ID NO:32) corresponding to the incorporated '007 application. The resulting 1.6 kb HA2 PCR product was cloned in an identical way as described for HA1, resulting in pcDNA2001/DHFRwt-swHA2.

Example 28

Integration of cDNAs Encoding Post-translational Modifying Enzymes

Since the levels of recombinant protein production in stable and transiently transfected and infected PER.C6 and PER.C6/E2A are extremely high and since a higher expression level is usually obtained upon DHFR dependent amplification due to increase of MTX concentration, an “out-titration” of the endogenous levels of enzymes that are involved in post-translational modifications might occur.

Therefore, cDNAs encoding human enzymes involved in different kinds of post-translational modifications and processes such as glycosylation, phosphorylation, carboxylation, folding and trafficking are being overexpressed in PER.C6 and PER.C6/E2A to enable a more functional recombinant product to be produced to extreme levels in small and large settings. It was shown that CHO cells can be engineered in which an alpha-2,6-sialyltransferase was introduced to enhance the expression and bioactivity of tPA and human erythropoietin (Zhang et al., 1998, Minch et al., 1995, Jenkins et al., 1998). Other genes such as beta 1,4-galactosyltransferase were also introduced into insect and CHO cells to improve the N-linked oligosaccharide branch structures and to enhance the concentration of sialic acids at the terminal residues (Weikert et al., 1999; Hollister et al., 1998). PER.C6 cells are modified by integration of cDNAs encoding alpha 2,3-sialyltransferase, alpha 2,6-sialyltransferase and beta 1,4-galactosyltransferase proteins to further increase the sialic acid content of recombinant proteins produced on this human cell line.

Example 29

Inhibition of Apoptosis by Overexpression of Adenovirus E1B in CHO-dhfr Cells

It is known that CHO cells, overexpressing recombinant exogenous proteins, are highly sensitive for apoptotic signals, resulting in a generally higher death rate among these stable producing cell lines as compared to the wild-type or original cells from which these cells were derived. Moreover, CHO cells die of apoptotic effects when agents such as lipofectamine are being used in transfection studies. Thus, CHO cells have a great disadvantage in recombinant protein production in the sense that the cells are very easily killed by apoptosis due to different reasons. Since it is known that the E1B gene of adenovirus has anti-apoptotic effects (White et al., 1992; Yew and Berk 1992), stable CHO-dhfr cells that express both heavy and light chains of the described antibodies (see, Examples 3, 4 and 5) are being transfected with adenovirus E1B cDNAs to produce a stable or transient expression of the E1B proteins to finally ensure a lower apoptotic effect in these cells and thereby increase the production rate of the recombinant proteins. Transiently transfected cells and stably transfected cells are compared to wild-type CHO-dhfr cells in FACS analyses for cell death due to the transfection method or due to the fact that they over-express the recombinant proteins.

Stable CHO cell lines are generated in which the adenovirus E1B proteins are overexpressed. Subsequently, the apoptotic response due to effects of, for instance, Lipofectamine in these stable E1B producing CHO cells is compared to the apoptotic response of the parental cells that did not receive the E1B gene. These experiments are executed using FACS analyses and commercially available kits that can determine the rate of apoptosis.

Example 30

Inhibition of Apoptosis by Overexpression of Adenovirus E1B in Human Cells

PER.C6 cells and derivatives thereof do express the E1A and E1B genes of adenovirus. Other human cells, such as A549 cells, are being used to stably overexpress adenovirus E1B to determine the anti-apoptotic effects of the presence of the adenovirus E1B gene as described for CHO cells (see, Example 29). Most cells do respond to transfection agents such as lipofectamine or other cationic lipids, resulting in massive apoptosis and finally resulting in low concentrations of the recombinant proteins that are secreted, simply due to the fact that only few cells survive the treatment. Stable E1B overexpressing cells are compared to the parental cell lines in their response to overexpression of toxic proteins or apoptosis inducing proteins and their response to transfection agents such as lipofectamine.

Example 31

Generation of PER.C6 Derived Cell Lines Lacking a Functional DHFR Protein

PER.C6 cells are used to knock out the DHFR gene using different systems to obtain cell lines that can be used for amplification of the exogenous integrated DHFR gene that is encoded on the vectors that are described in Examples 1 to 5 or other DHFR expressing vectors. PER.C6 cells are screened for the presence of the different chromosomes and are selected for a low copy number of the chromosome that carries the human DHFR gene. Subsequently, these cells are used in knock-out experiments in which the open reading frame of the DHFR gene is disrupted and replaced by a selection marker. To obtain a double knock-out cell line, both alleles are removed via homologous recombination using two different selection markers or by other systems as, for instance, described for CHO cells (Urlaub et al., 1983).

Other systems are also applied in which the functionality of the DHFR protein is lowered or completely removed, for instance, by the use of anti-sense RNA or via RNA/DNA hybrids, in which the gene is not removed or knocked out, but the down stream products of the gene are disturbed in their function.

Example 32

Long-term Production of Recombinant Proteins Using Protease and Neuraminidase Inhibitors

Stable clones described in Example 8 are used for long-term expression in the presence and absence of MTX, serum and protease inhibitors. When stable or transfected cells are left during a number of days to accumulate recombinant human EPO protein, a flattening curve instead of a straight increase is observed, which indicates that the accumulated EPO is degraded in time. This might be an inactive process due to external factors such as light or temperature. It might also be that specific proteases that are produced by the viable cells or that are released upon lysis of dead cells digest the recombinant EPO protein. Therefore, an increasing concentration of CuSO₄ is added to the culture medium after transfection and on the stable producing cells to detect a more stable production curve. Cells are cultured for several days and the amount of EPO is determined at different time points. CuSO₄ is a known inhibitor of protease activity, which can be easily removed during down stream processing and EPO purification. The most optimal concentration of CuSO₄ is used to produce recombinant human EPO protein after transient expression upon DNA transfection and viral infections. Furthermore, the optimal concentration of CuSO₄ is also used in the production of EPO on the stable clones. In the case of EPO in which the presence of terminal sialic acids is important to ensure a long circulation half-life of the recombinant protein, it is necessary to produce highly sialylated EPO. Since living cells produce neuraminidases that can be secreted upon activation by stress factors, it is likely that produced EPO lose their sialic acids due to these stress factors and produced neuraminidases. To prevent clipping off of sialic acids, neuraminidase inhibitors arc added to the medium to result in a prolonged attachment of sialic acids to the EPO that is produced.

Example 33

Stable Expression of Recombinant Proteins in Human Cells Using the Amplifiable Glutamine Synthetase System

PER.C6 and derivatives thereof are being used to stably express recombinant proteins using the glutamine synthetase (GS) system. First, cells are being checked for their ability to grow in glutamine-free medium. If cells cannot grow in glutamine-free medium, this means that these cells do not express enough GS, finally resulting in death of the cells. The GS gene can be integrated into expression vectors as a selection marker (as is described for the DHFR gene) and can be amplified by increasing the methionine sulphoximine (MSX) concentration resulting in overexpression of the recombinant protein of interest, since the entire stably integrated vector will be co-amplified as was shown for DHFR. The GS gene expression system became feasible after a report of Sanders et al. (1984) and a comparison was made between the DHFR selection system and GS by Cockett et al. (1990). The production of recombinant mAbs using GS was first described by Bebbington et al. (1992).

The GS gene is cloned into the vector backbones described in Example 1 or cDNAs encoding recombinant proteins and heavy and light chains of mabs are cloned into the available vectors carrying the GS gene. Subsequently, these vectors are transfected into PER.C6 and selected under MSX concentrations that will allow growth of cells with stable integration of the vectors.

Example 34

Production of Recombinant HIV gp120 Protein in a Human Cell

The cDNA encoding the highly glycosylated envelope protein gp120 from Human Immunodeficiency Virus (HIV) is determined and obtained by PCR using primers that harbor a perfect Kozak sequence in the upstream primer for proper translation initiation and convenient restriction recognition sequences for cloning into the expression vectors described in Example 1. Subsequently, this PCR product is sequenced on both strands to ensure that no PCR mistakes are being introduced.

The expression vector is transfected into PER.C6, derivatives thereof and CHO-dhfr cells to obtain stable producing cell lines. Differences in glycosylation between CHO-produced and PER.C6 produced gp120 are being determined in 2D electrophoresis experiments and subsequently in Mass Spectrometry experiments, since gp120 is a heavily glycosylated protein with mainly O-linked oligosaccharides. The recombinant protein is purified by persons skilled in the art and subsequently used for functionality and other assays. Purified protein is used for vaccination purposes to prevent HIV infections.

Example 35

Cloning of Expression Vectors Encoding Factor VIII

Routine molecular biology methods were used to clone a full length and a B-domain deleted Factor VIII coding region into an expression vector. Briefly, separate cDNA fragments roughly coinciding with the A, B and C domains of factor VIII, and together covering the complete coding region of human factor VIII were obtained by PCR on human liver cDNA. These fragments were inserted into suitable PCR product cloning vectors and the constructs were sequenced to verify their integrity. The cloned fragments were used as templates to assemble both the full length factor VIII coding region (7.1 kb), as well as a B-domain deleted factor VIII coding region (4.4 kb, named the SQ variant; Lind et al., 1995). The reassembled coding regions were each inserted into expression vector pcDNA2001Neo (supra), to generate the final expression constructs. The expression vector containing the full length factor VIII coding sequence is named pCP-FactorVIII-FL, and the expression vector containing the B-domain-deleted factor VIII coding sequence is named pCP-FactorVIII-SQ. Both are depicted in FIG. 1. The factor VIII coding sequence in these plasmids is under control of the CMV promoter (see, e.g., U.S. Pat. No. 5,168,062; WO 03/051927) and is followed by a bovine growth hormone (bGH) polyA signal (see U.S. Pat. No. 5,122,458). Sequence analysis of the inserts of the final expression vectors pCP-FactorVIII-SQ and pCP-FactorVIII-FL confirmed that all FactorVIII coding sequences correspond to the reference sequence (RefSeq, acc. nr. NM_(—)000132) of FactorVIII as present in Genbank (http://www.ncbi.nlm.nih.gov/entrez/query.fcgi).

Initial experiments showed that after transfection into PER.C6 cells, both vectors gave rise to factor VIII expression. The levels observed with the full length construct were very low. Further experiments were performed with the B-domain deleted variant, which is also slightly easier to handle.

Example 36

Generation of BDD-SQ Variant FVIII Expressing PER.C6 Cell Lines

PER.C6 cells were transfected with plasmid pCP-FactorVIII-SQ (see Example 35). Transfections were performed using LipofectAMINE™ according to the manufacturer's instructions. In brief, PER.C6 cells were seeded in 22 tissue culture dishes (10 cm diameter) containing DMEM plus 10% FCS at 3.5×10⁶ cells per dish. The cells were seeded on the day prior to transfection and cultured overnight at 37° C. and 10% v/v CO₂. At day 1, cells were transfected using 10 μl LipofectAMINE™ and 2 μg DNA (pCPFactorVIII-SQ) per dish. Culture medium containing 0.5 mg/ml Geneticin® was replaced after four hours and refreshed every two to three days.

Individual neomycin resistant clones were picked at day 20 and seeded into 96-well plates. The factor VIII concentration from 352 clones was determined in the first screen by Coatest VIII:C/4 (Chromogenix AB, Molndal, Sweden). From this screen, 124 clones were carried forward to a second screen. This test was performed in 96-well plates and supernatants were harvested after seven days. From this screen, the 40 highest producing clones were selected and analysed in six-well plates. Each clone was seeded at 0.5×10⁶ cells per well (in duplicate) and incubated for two days at 37° C. and 10% CO₂. The medium was then replaced with fresh culture medium and incubated for another day at 37° C. and 10% CO₂. The supernatant of each well was then harvested and FVIII concentration directly measured by CoatestVIII;C/4. From this screen, six high producing clones were identified (Table 1), with productivities ranging from 1.7 to 3.2 U/10⁶ cells/day. The highest producing cell line (SQ 242) was selected for further characterisation.

Example 37

BDD-SQ-FVIII Produced in Serum-Free Media

Batch cultures of SQ-242 were initiated in 250 ml Ehrlenmeyer shake flasks (Corning) containing 30 ml of either ExCell VPRO or ExCell Mab serum-free medium (both from JRH Biosciences). Cells were seeded at 1, 2 or 3×10⁶ viable cells/ml and incubated on an orbital shaker (Infors) at 100 rpm in a humidified incubator at 37° C. and 5% (v/v) CO₂. Samples were taken at t=1, 2, 4 and 8 hours. Supernatants were frozen immediately on dry ice and stored at −80° C. until analysis in a chromogenic assay (Coatest, Chromogenix). FIG. 2 and Table 2 show that the cell specific productivity of the cell line SQ 242 in both commercially available serum-free media was similar at approximately 2.2-3.5 U/10⁶ cells/day. The specific productivity was calculated from the slope of the plots of FVIII concentration against the integral of the viable cell concentration (IVC).

Example 38

Determination of Specific Productivity in VPRO Medium 24-Hour Batch Cultures

Batch cultures of SQ 242 were initiated in 250 ml Ehrlenmeyer shake flasks (Coming) containing 30 ml ExCell VPRO serum-free medium (JRH Biosciences). Cells were seeded in duplicate flasks at viable cell concentrations of 1, 2, 4, 8 and 12×10⁶ per ml. Cultures were sampled at t=1, 2, 4, 8 and 24 hours. Supernatants were frozen immediately on dry ice and stored at −80° C. until analysis in a chromogenic assay (Coatest, Chromogenix). The viable cell concentration was determined using a CASY TT (Schaerfe Systems).

After 24 hours, a complete medium change was performed, the cultures were seeded into fresh shake flasks at the same starting cell concentration (1, 2, 4, 8, and 12×10⁶ cells/ml respectively) and a second 24-hour batch culture was initiated. Results are summarized in FIGS. 3-5 and Table 3. FIG. 4 shows the accumulation of DBB-FVIII SQ over 24 hours. At viable cell concentrations of 1 and 2×10⁶ cells/ml, FVIII accumulated over the 24-hour culture period. However, at the higher cell concentrations, FVIII accumulated up to eight hours (for 4 and 8×10⁶ cells/ml) and four hours (12×10⁶ cells/ml). Over the following 16 to 20 hours, a decrease in product concentration was observed. The period of product accumulation at each cell concentration was plotted against the integral of the viable cell concentration (FIG. 5). The slope of these plots was used to calculate the cell specific productivity. The specific productivity calculated over these periods for all cell concentrations tested was similar as in Example 37, at 2.7-3.8 U/10⁶ cells/day.

2-Hour Medium Change Cultures

Cultures were initiated in 250 ml Ehrlenmeyer shake flasks (Corning) containing 30 ml ExCell VPRO serum-free medium (JRH Bioscience). Cells were seeded in duplicate flasks at viable cell concentrations of 1, 2, 4, 8 and 12×10⁶ per ml. A complete medium exchange was performed for all cultures at t=2, 4 and 6 hours. Harvested culture supernatants were frozen immediately on dry ice and stored at −80° C. until analysis in a chromogenic assay (Coatest, Chromogenix). The viable cell concentration was determined in a CASY TT (Schaerfe Systems, GMBH).

After the medium exchange performed at t=6 hours, cells were seeded into fresh shake flasks and incubated overnight. At t=24 hours, a complete medium change was performed, the cultures were seeded into fresh shake flasks at the same starting cell concentration (1, 2, 4, 8, and 12×10⁶ cells/ml respectively) and a second series of medium changes performed at t=26, 28 and 30 hours. Harvested culture supernatants were frozen immediately on dry ice and stored at −80° C. until analysis in a chromogenic assay (Coatest, Chromogenix). Results are summarized in FIGS. 6 and 7 and Table 4. Cell specific productivity was calculated from each 2-hour culture period, plotting the FVIII concentration against the integral of the viable cell concentration. Values at 1, 2, 4 and 8×10⁶ cells/ml were similar at 2.3-5.4 U/10⁶ cells/day. Values at 12×10⁶ cells/ml were somewhat lower, at 1.3 U/10⁶ cells/day.

Tables TABLE 1 Six selected cell lines expressing BDD-FVIII-SQ Volumetric production Cell specific production (U/ml/24 hours) (U/10⁶ cells/24 hours) Clone ID Factor VIII-SQ Factor VIII-SQ SQ-078 5.50 2.01 SQ-115 5.20 1.76 SQ-167 3.55 1.72 SQ-187 2.00 2.05 SQ-231 4.02 1.63 SQ-242 9.26 3.18

TABLE 2 Summary of BDD-SQ-FVIII production in Mab and VPRO media FVIII produced in 8 hours Specific productivity Medium (U/ml) (U/10⁶ cells/d) Mab (1 × 10⁶ cells/ml) 1.15 2.6 (1.0-1.3) VPRO (1 × 10⁶ cells/ml) 1.35 3.5 (1.4-1.5) VPRO (2 × 10⁶ cells/ml) 2.15 2.2 (2.0-2.3) VPRO (3 × 10⁶ cells/ml) 3.55 3.3 (3.1-4.0)

TABLE 3 Maximum Factor VIII production during 24-hour batch cultures Time point at which Specific Cell Maximum FVIII maximum FVIII productivity concentration concentration concentration (U 10⁶ cells⁻¹ (10⁶ ml⁻¹) (U/ml) measured (hours) day⁻¹) 1 4.4 24 3.4 (3.9-4.9) 2 8.4 24 3.2 (7.8-8.9) 4 5.3 8 3.6 (4.5-7.0) 8 5.0 8 3.8 (4.1-5.7) 12 5.6 4 2.7 (4.4-8.1)

TABLE 4 Maximum Factor VIII production during 24-hour batch culture with medium change every 2 hours Cell Maximum FVIII concentration concentration in each 2-hour culture period Specific productivity (10⁶ ml⁻¹) (U/ml) (U 10⁶ cells⁻¹ day⁻¹) 1 0.45 5.2 (0.3-0.7) 2 0.82 5.4 (0.5-1.0) 4 1.46 4.4 (1.0-1.9) 8 1.50 2.3 (1.0-2.0) 12 1.15 1.3 (0.7-1.6)

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1. A process for recombinant production of blood coagulation Factor VIII in an immortalized human embryonic retina cell, said cell expressing at least an adenoviral E1A protein and comprising a nucleic acid sequence encoding said Factor VIII, said nucleic acid sequence being under control of a heterologous promoter, said process comprising: culturing said immortalized human embryonic retina cell and expressing the Factor VIII in said cell; and harvesting the expressed Factor VIII.
 2. The process of claim 1, wherein said immortalized human embryonic retina cell further expresses at least one adenovirus E1B protein.
 3. The process of claim 1, wherein said immortalized human embryonic retina cell is a PER.C6 cell such as deposited under ECACC no.
 96022940. 4. The process of claim 1, wherein said Factor VIII has a deletion in the B-domain.
 5. The process of claim 5, wherein said Factor VIII with a deletion in the B-domain is the Factor VIII SQ mutant.
 6. The process of claim 1, wherein said immortalized human embryonic retina cell does not express an adenoviral structural protein.
 7. The process of claim 1, wherein said heterologous promoter is a cytomegalovirus (CMV) immediate early promoter.
 8. The process of claim 1, wherein the culturing is performed in serum-free culture medium.
 9. The process of claim 1, wherein the culturing is performed in a process chosen from the group consisting of a batch culture process, a fed-batch culture process, a perfusion culture process, and a combination of two or more of these.
 10. The process of claim 4, wherein the specific productivity of Factor VIII with a deletion in the B-domain is at least 0.1 Unit×10⁶ cells⁻¹×24 hours⁻¹.
 11. The process of claim 4, wherein the specific productivity of Factor VIII with a deletion in the B-domain is at least 0.5 Unit×10⁶ cells⁻¹×24 hours⁻¹.
 12. The process of claim 4, wherein the specific productivity of Factor VIII with a deletion in the B-domain is at least 1.0 Unit×10⁶ cells⁻¹×24 hours⁻¹.
 13. An immortalized human embryonic retina cell, comprising: a genome; a nucleic acid sequence encoding an adenoviral E1A protein, wherein the nucleic acid sequence encoding the adenoviral E1A protein is integrated in the genome; and a nucleic acid sequence encoding blood coagulation Factor VIII under control of a heterologous promoter, wherein the nucleic acid sequence encoding blood coagulation Factor VIII under control of a heterologous promoter is integrated in the genome of the immortalized human embryonic retina cell.
 14. The immortalized human embryonic retina cell of claim 13, wherein said Factor VIII has a deletion in the B-domain.
 15. The immortalized human embryonic retina cell of claim 14, wherein said Factor VIII with a deletion in the B-domain is the Factor VIII SQ mutant.
 16. The immortalized human embryonic retina cell of claim 13, wherein said heterologous promoter is a cytomegalovirus (CMV) immediate early promoter.
 17. The immortalized human embryonic retina cell of claim 13, further comprising a sequence encoding an adenoviral E1B protein integrated in its genome.
 18. The immortalized human embryonic retina cell of claim 13, wherein said immortalized human embryonic retina cell does not comprise a nucleic acid sequence encoding an adenoviral structural protein in its genome.
 19. The immortalized human embryonic retina cell of claim 13, wherein the immortalized human embryonic retina cell is a PER.C6 cell such as deposited under ECACC no.
 96022940. 20. A process for producing blood coagulation Factor VIII, said process comprising: culturing the immortalized human embryonic retina cell of claim 13; and expressing blood coagulation Factor VIII.
 21. The process of claim 20, further comprising: isolating, purifying, or isolating and purifying blood coagulation Factor VIII from said immortalized human embryonic retina cell, from a culture medium associated with said immortalized human embryonic retina cell, or a combination thereof.
 22. The process of claim 20, wherein said culturing is performed in a serum-free culture medium and the immortalized human embryonic retina cell is in suspension during said culturing.
 23. The process of claim 20, wherein said culturing is performed in a process chosen from a batch culture process, a fed-batch culture process, a perfusion process, and a combination of two or more of these. 24-32. (canceled) 